Method of processing bio-mass matter into renewable fluid fuels (synthetic diesel)

ABSTRACT

The present invention relates to improved production methods and production equipment for fluid fuels including but not limited to ethanol, gasoline, hydrogen, naphtha (for olefin manufacture) and/or diesel but most particularly, “designed” synthetic diesel fuels for use in corresponding diesel engines. Apparatus and methods for producing the fluid fuels are described.

CROSS-REFERENCE TO RELATED PATENT APPLICATIONS

This application incorporates by this reference U.S. ProvisionalApplication No. 60/783,963, filed Mar. 20, 2006; U.S. ProvisionalApplication No. 60/786,959, filed Mar. 29, 2006; U.S. ProvisionalApplication No. 60/799,515, filed May 11, 2006. This application is aContinuation-In-Part of U.S. application Ser. No. 11/490,861, filed Jul.21, 2006, incorporated herein by reference in its entirety. Thisapplication claims priority from Provisional Application U.S.Application 60/931,837, filed May 25, 2007, incorporated herein byreference in its entirety. This application claims priority fromProvisional Application U.S. Application 60/950,249, filed Jul. 17,2007, incorporated herein by reference in its entirety. This applicationclaims priority from Provisional Application U.S. Application60/953,741, filed Aug. 3, 2007, incorporated herein by reference in itsentirety. This application claims priority from Provisional ApplicationU.S. Application 60/967,658, filed Sep. 6, 2007, incorporated herein byreference in its entirety.

BACKGROUND OF THE INVENTION

The present invention relates to improved production methods andproduction equipment for fluid fuels including but not limited toethanol, gasoline, hydrogen, naphtha (for olefin manufacture) and/ordiesel but most particularly, “designed” synthetic diesel fuels for usein corresponding diesel engines. Diesel of any Cetane value, such asdiesel having a formula range between the following Cetane values:(C₁₀H₂₂), to (C₁₅H₃₂); and including diesel fuel with higher (greater)and/or lower Cetane values, are the most important but also any type ofgasoline, ethanol can be readily and most economically manufactured fromrenewable bio-mass sources. Additionally, the production of largevolumes of hydrogen gas (H₂) can be co-produced as a primary orsecondary byproduct for any applicable use but most importantly for fuelrequired by hydrogen cell powered vehicles. The above referenced fluidfuels plus many others, are manufactured by synthesizing syn-gas (ablend of gases including CO and H₂ in any suitable proportions and whichmay include some CO₂ and H₂O vapor), the ratio of gases relative to eachother can be “trimmed” (an industry term meaning adjustment of thereferenced ratio between the gases and, most likely between the CO andH₂ content of the syn-gas to provide for greater production efficiencyof the fluid fuel(s) sought); such “trimming” may be achieved byexposure or direct contact with a suitable catalyst(s). Alternatively,the syn-gas can be transferred through a single or series of membrane(manufactured, for example, from a polypropylene or other polyolefinextruded and “blown” film to provide a membrane tube) conduits which inturn, is enclosed in larger diameter conduit maintained at a selectedpressure and temperature such as 50 psi and 90° C. to reduce anexcessive proportion of hydrogen gas.

In particular, the present patent application relates to the field ofrenewable fluid fuel production methods as required for use in internalcombustion engines, jet engines and turbines typically installed inautomobiles, buses, trucks, railroad locomotives, ships and airplanes.

The field of invention also includes the production equipment requiredfor the manufacture of the fluid fuels but also other liquids such asnaphtha and lubricating oils of any type including timber treatment oilsand/or varnishes, stain removers (from clothes) and engine cleaningfluids able to dissolve and remove other oils, dirt and grime from anengine; any other Fischer Tropsch fluids can also be produced with thereferenced production equipment.

The primary purpose, however, for developing the herein specifiedproduction equipment and methods for manufacturing the fuels disclosedis to facilitate displacement of fossil fuels (including any type ofcoal including soft wet fuels such as peat and lignite through to thehardest black anthracite, which are presently consumed in massivequantities during operation of the vehicles indicated above and electricpower production, in what appears to be exponentially increasingquantities. Such production of renewable fuels and liquids indicatedabove, from biomass material sources can facilitate a correspondingreduction in the release of greenhouse gases presently released by thedirect, typically untreated exhausting into Earth's atmosphere.

SUMMARY OF THE INVENTION

The present invention provides a reliable, reproducible, and costeffective method of fluid fuels manufacture by synthesizing syn-gas innovel and more efficient steam reforming equipment and Fischer Tropschsynthesizing reactors, for the production of said syn-gas by equipmenthoused within standard containerized configuration of substantiallyreduced size when compared to gasification and Fischer Tropschinstallations built by others.

The invention disclosed herein includes carbon steam reforming equipmentintegrated with Fischer-Tropsch [F-T] reactors of small to medium output(wherein firstly; for example, a large output, commercial system,including a Fluidized Bed, Steam Reformer integrated with acorrespondingly sized F-T system, and a production capacity of 200,000barrel per day (BPD) of refined fluids production out-put, with airseparation equipment of adequate production capacity to providesufficient (greater than 100 tons per day) oxygen gas; the O₂ isinjected directly into the fluidized bed combustion chamber, therebyburning sufficient crude oil or natural gas feed stock, to drive thesteam reforming reactions (listed below) with suitable F-T productionequipment costs approximately US $4 billion to US $5 billion [includingair separation equipment for pure oxygen supply to the steam reformer];and a medium sized steam reforming and F-T system of 20,000 BPD outputcosts about $25,000 per single BPD output equal to approximately $0.5billion cost).

The present invention, having a production capacity of about 1,000 BPDand costing about US $5 to $9 million for each system is disclosedherein with methods of utilizing block heat storage to, most preferably,use “off peak” green or hydro electricity as opposed to burning a largecomponent of the bio-mass feed-stock to correspondingly generateadequate heat to drive the endothermic steam reforming reactions. Inaddition, by installing small renewable fuels production systemsregionally, when located in complete, operable facilities, built acrossthe USA, with each system having sufficient capacity to satisfy the fuelneeds of the entire respective regions population fuel needs, the costof each gallon of fuel should be lower than as it is presently. Thepresent method of renewable fuel production, as disclosed herein, ismost preferably located as close as possible to one or more of thenumerous biomass sources within the USA such as, and most preferably,close to the logging industries of the Pacific North West (PNW) forestsand additionally, adjacent to one of the many hydro electric damslocated along the Columbia River and its tributaries. Renewable fuelcosts, produced in this way, can be most competitive when compared withthe full, actual costs of fossil fuels derived from crude oil sourcedfrom Middle Eastern oil wells; these include among other costs; thetotal deep water or deep ground crude oil extraction costs from deepdrilled wells, military equipment and costs of personnel (human life)costs, shipping, the higher refining of lower grade, high sulfur contentcrude oil, further pipeline and/or trucking transport costs associatedwith delivery to the final point of sale and consumption, plus themassive loss of cash, paid to the benefit of the oil well owners oftenresiding in remote locations of foreign lands.

When compared with the highly efficient conversion method of wet biomass(wherein water contained is a reactant in the steam reforming productionof syn-gas) to renewable fuels, wherein the source of endothermic,reaction supporting, heat is provided by electricity generated duringthe “off peak” periods of each day, stored in high temperature liquefiedmetals such as aluminum or copper; or pressurized zinc or tin, held inpressure vessels so as to elevate the boiling point of the metals which,in one preferred embodiment, are maintained within a temperature rangebetween a low of 700° C. and a high of 1,200° C. Other metals used as“block heat storage banks” may comprise a single electric heatingelement but most preferably a mixture of molten metal's, selected fromthe list herein below disclosed or others not listed but in any eventthe molten metal(s) is enclosed within a sealed, substantiallyleak-proof, insulated vessel manufactured from suitable materials suchas nickel aluminite (NiAl), Inconel or Incoloy (Registered trade marks)a combination thereof or any other suitable materials. A stream ofsuitably trimmed syn-gas, produced according to the methods disclosedherein, utilizing equipment also disclosed and arranged for convenientinstallation, transport and operation (NB: equipment may be skid mountedwithin a series of 20′FCL (shipping containers and/or 40′FCLfoot-printed skids, facilitating relocation and rapid installation ofthe complete set of equipment required to produce syn-gas as required.The stream of syn-gas is then transferred via a conduit under suitablepressure to a Fischer Tropsch reactor comprising an enclosed spacecontaining a selected catalyst (or catalysts) arranged within a firstspace, mounted onto a framework which is, itself, mounted onto acentrally disposed, vertically oriented shaft so as to enable motordriven rotation or spinning of the framework (within said first spaceand catalyst attached thereto). The conduit, within which said syn-gasis transferred, is connected so as to direct the syn-gas into theconduit provided by a hollow shaft 802 as is shown in FIG. 6( ii).

A homogenizer, for example, a high pressure homogenizer is integratedinto the biodiesel production system. The homogenizer can be insertedbetween the upstream colloid mill (in which the combined input stream ofCO₂, ethanol and triglyceride streams are thoroughly “preblended”), andthe downstream reactor microchannel, for the purpose of insuring thecomplete mixing and elimination of any “d-mixing” or separation of thetriglycerides from the super critical ethanol and the CO₂ solvent. Thecolloid mill may be located on either side of the homogenizer (i.e.,upstream or downstream thereof). One example of the homogenizer that canbe used is a very high pressure homogenizer manufactured by Niro, Inc.in Columbia, Md. It should be understood that other types ofhomogenizers and additional related equipment can be integrated into thebiodiesel production system.

The bio-mass, may include, bagasse, sugar beet waste, canned corn orvegetable waste, cotton waste, sewage sludge, wheat straw, tree trunkbark and associated branches, and the roots of harvested trees, hay(such as is grown in the Pacific North West and most notably Oregon forgrass seed production) and/or rice straw. Irrespective of the bio-masssource it is converted to carbon, water and ash with electricallypowered heating in specially modified extruders (typically used inplastics sheet production).

The centralized production of transport fuels in massive quantities alsorequires distribution to consumers often located in remote regionsrelative to the point of production and is shipped, typically, via longdistance road transport and/or rail shipping to consumers and industry.This present production method for synthesized fuels and plastics rawmaterial production, has been built with complete gasification andFischer Tropsch synthesizing systems with 10,000 BPD, 20,000 BPD up to200,000 BPD or more—Barrels Per Day (BPD) or equivalent input capacitiesof crude oil, lignite or coal input streams which, until now have beenconsidered the lowest quantities so as to avoid inefficiencies inprocessing such commodities into diesel, gasoline, methanol or naphtha,which have become inefficient due to the steady increase in costs of theimported raw materials from countries that are at best, with fewexceptions, considered unreliable and politically unstable, and inaddition, are located great distances from the most significant marketsfor the processed and finished commodities. Massive shipping tankersendanger the ecosystems through which they regularly travel to deliverwhat has become a continually increasing, exceedingly expensivecommodity. It is now clear that “economies of scale” for production ofrenewable fuels from biomass has become competitive and with much lowerquantity input BPD equivalents (except for oxygen production which isnormally required to facilitate the use of the respective input [i.e.biomass, lignite, coal etc.] raw material for the massive heatingrequired by way of combustion; in this way heat can be readily provided(to enable the gasification of the raw material input) by injectingmeasured amounts of pure oxygen into the gasification pressure vesselwith the natural gas and/or black coal raw materials. Regionalproduction that utilizes zero to low cost, but relatively much smallerquantities of locally available biomass raw materials not only requiresefficient and affordable equipment but this equipment must besubstantially smaller in scale and of much lower cost when compared tothe massive plant that is now populating the regions where low costnatural gas is available. Furthermore the equipment required forregional production of biomass to liquid (BTL) fuels must be efficientwhile producing relatively small quantities of fuel for localconsumption such as in rural and agricultural communities across the USAand in those regions furthest from existing fuel processing facilitiesin addition to having adequate quantities of biomass materials requiredsuch as animal waste and crop stover and straw etcetera. Additionallythe equipment can also be employed to convert the massive waste streamsemanating from the densely populated cities. Such waste streams comprisepaper and board, plastics such as polyethylene packaging, and plasticshaving become too contaminated to recycle etcetera. The disclosureherein also includes a method of CO₂ collection such as the massive CO₂exhaust streams from coal powered electric power production facilitiesand also CO₂ from fermentation processes used in ethanol production andalso alcohol production for human consumption, albeit that these CO₂streams are not derived directly from the burning of fossil fuels. Thecollection of CO₂ from any source provides an opportunity to reducecarbon emissions resulting from human endeavor and then thesequestration of, for example, the liquefied CO₂ by high pressure (up toand even greater than 14,000 psi), positive displacement, pumpingdirectly down the shaft and into suitable low production or sealed andabandoned oil wells which may result in an opportunity to recover acorresponding quantity of fossil fuel from a USA source resulting in thedisplacement of an equal amount of imported crude oil.

There is further provided a method of gasifying a blend of raw materialsto produce a syn-gas, in preparation for synthesizing, in large part,renewable fluid bio-fuel, most preferably comprising a high cetaneDiesel. Aviation fuel and plastics raw material feedstock (i.e. naphtha,from which for example, polyolefin plastics such as polyethylene andpolypropylene can be manufactured—in which case there would be at leasttwo fluid products synthesized, including synthetic Diesel and Aviationfuel [C_(n)H₂₊₂], and naphtha [having an averaged formula ofapproximately C₈H₁₈]. Wherein said synthesized fluids are derived from afirst stream of super heated steam at a selected temperature between600° C. and 1,400° C., but most preferably about 1,000° C. andcontrolled pressure up to 200 bar or greater, arranged so that a second,similarly heated and pressurized stream of gaseous CO₂ are combinedtogether and transferred via an electrically heated conduit. The conduitcan be fabricated from Inconel 625 or similar metal able to tolerate theselected temperature and pressure conditions. The mixture is transportedto a first electrically heated, enclosed and sealed reactor which isalso maintained at a selected temperature and pressure. Providing athird anoxic stream of pulverized carbon derived from any suitablesource such as pet-coke and/or suitable coal such as black subituminous,oxygen free and powdered so as to ensure said pulverized particles donot exceed about 200 microns across the widest dimension. An electricitysupply for heating said first, second and third streams and equipment asrequired is most preferably provided directly from wind turbinegenerator sources or alternatives such as solar, tidal, hydrocontrolling the relative proportions of said first, second and thirdstreams, NB: electric supply is equivalent to about 34% of all energy ina mass balance equation including said three streams and all matterrequired. In this way the installation of an air separator for supply ofthe corresponding quantity of oxygen is no longer needed and theadditional carbon or coal that would otherwise be provided to enablecombustion of the coal transferred with the gases into the reactor burnand provide the heat needed for the reactor. Anoxic conditions arerequired within the conduits and vessels through which the productstream, through to finished fluids are transferred. Pulverizedcarbon/coal and/or PET coke particles of about <200 microns at widestdimension. Note: PET-coke, typically a 90% carbon content solid residue,but carbon content decreases with lower grade crude oil, periodicallyextracted from crude oil refining equipment.

BRIEF DESCRIPTION OF THE DRAWINGS

The foregoing aspects and many of the attendant advantages of thisinvention will become more readily appreciated by reference to thefollowing detailed description, when taken in conjunction with theaccompanying drawings, wherein:

FIG. 1 shows in diagrammatic format a cross section through severalitems of equipment according to the present invention;

FIG. 1( i) shows a cross section through the vertical plane intersectingthe center line of centrally located shaft of a Fischer-Tropsch reactorarranged according to the present invention;

FIG. 1( ii) shows a horizontal cross section through the Fischer-Tropschreactor of FIGURE (i), arranged according to the present invention;

FIG. 1( iii) shows a vertical cross section through a segment (Area “A”)of the Fischer-Tropsch reactor, of FIGURE (i), arranged according to thepresent invention;

FIG. 2 shows a cross section bisecting the vertical plane intersectingthe center line of a centrally located shaft of a Fischer-Tropschreactor arranged according to the present invention;

FIG. 3 shows an isometric view of gasification equipment comprising anelongated pressure vessel enclosing a first, spiraled, conduit sectionmanufactured from high temperature (900° C.+) tolerant steel, connectedat the upper end of a second, straight, conduit section of similar crosssectional dimensions to said first conduit, located centrally having acommon center line with said enclosing vessel, and a horizontal, third,straight conduit section connected to the lower end of said firstconduit section, according to according to the present invention;

FIG. 3( i) shows a cross section “X”-“X” through the gasificationequipment of FIG. 3, according to the present invention;

FIG. 4 shows a diagrammatic side view outline of equipment assembled forthe selective collection and reduction to liquid of carbon dioxide gasfrom engine or furnace exhaust according to the present invention;

FIG. 6 shows a partial cross section side view of equipment designed forthe gasification of pulverized carbon according to the presentinvention;

FIG. 6( i) illustrates a cross-section view of several gasification ofpulverized carbon devices;

FIG. 6( ii) shows a cross section through the vertical planeintersecting the center line of centrally located shaft of aFischer-Tropsch reactor arranged according to the present invention;

FIG. 7 shows a diagrammatic plan view of the outline of equipment,represented by boxes and circles, arranged to show the normal operatinglocation of the equipment relative to each equipment component whereinthe equipment is arranged to convert organic, biomass feedstock torenewable fuels such as diesel according to the present invention;

FIG. 8 shows a partial cross sectioned side view, through the centerlineof an enclosed, tubular profiled pressure vessel with hemispherical endcaps of equipment designed for the gasification of pulverized carbon bythe steam reforming method according to the present invention;

FIG. 8( i) shows a cross section to show the construction of the wallcomposition of the pressure vessel represented by item 5012 in FIG. 7according to the present invention;

FIG. 9 shows a cross section side view, through the centerline of anenclosed, tubular profiled pressure vessel with hemispherical end capsof equipment with upper and lower enclosing heat exchangers arranged forthe gasification of pulverized carbon by the steam reforming methodaccording to the present invention;

FIG. 9( i) shows a cross section side view, through the centerline of anenclosed, tubular profiled pressure vessel with hemispherical end capsof equipment with upper and lower enclosing heat exchangers arranged forthe gasification of pulverized carbon by the steam reforming methodaccording to the present invention;

FIG. 10 is a cross-section of a cyclone through its centerline includinga connecting upper conduit, a lower connecting conduit and an integratedinput volute.

FIG. 11 is a schematic diagrammatic illustration of exemplaryembodiments of various industrial processes and equipment used toproduce liquid fuel emission products from coal fired electricitygenerating plants.

FIG. 12 is a cross-section of an exemplary embodiment of an apparatus tomix and homogenize fluids used in the production of bio-diesel fuel.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

FIG. 1 illustrates, in diagrammatic form, the general layout of aninstallation of equipment for the production of synthetic bio-fuelsderived from virtually any biomass and providing an opportunity tomanufacture renewable fuels as an alternative to fossil fuels. Therenewable fuels, produced from vegetation matter, can be used asalternatives to diesel or gasoline and also, and by way of example,polyolefin (polyethylene) plastics can be synthesized from a basefeedstock, naphtha or ethylene which is a liquid at ambient conditionsby, and in particular the polyolefin group of plastics includingpolypropylene, low density and high density polyethylene, and others.

The reaction is catalyzed by metals such as platinum, nickel, tungsten,chrome, ruthenium and molybdenum.

In a preferred embodiment, the process disclosed herein comprisescatalyst lined temperature controlled channels, such as the channelrepresented by the space between member 33 and disc 34 of FIG. 2 whichmay not exceed about 100 microns and through which syn-gas can be pumpedin the direction showed by arrow 38, at a selected temperature of about240° C. and pressure controlled by said pump at about 200 psi, with thetemperature controlled by disc profiled heat exchanger 33 is for theconversion of any biomass, but in particular a biomass sometimesreferred to as “Brewers Mash” and derived during the production ofethanol in a fermentation process wherein corn is the primary source ofthe sugars required and which yields a large quantity of “Brewers-Mash”and corn oil. The corn oil can be separated from the brewer's mash andconverted to bio-diesel using the methods disclosed in the abovereferenced patent applications. Ethanol derived from the fermentationprocess of the corn is combined with the corn oil with a quantity ofcarbon dioxide transferred through a micro channel heat exchangersimilar to the equipment described in association with FIG. 2 herein ata suitable pressure such as about 2,500 psi and temperature such asabout 150° C. to 250° C., resulting in production of bio-diesel andglycerol. The glycerol is separated from the bio-diesel and retained ina suitable storage vessel until required in a process for the preparingof the biomass associated with FIG. 1 herein. The equipment shown inFIG. 1 in diagrammatic format is a side view cross sectional diagramillustrating each component and the manner in which it is interfaced andconnected to the adjacent components. Each component performs a requiredprocess and when the equipment is installed in the way shown syn-gas(synthesis gas, or water gas) comprising hydrogen (H₂) and carbonmonoxide (CO), ash and other minor metals representing a very smallpercentage of the total input and the metals are relatively rare, suchas potassium, sodium etcetera. In general, a CO:H₂ ratio of about 55:45or 2.0:1.61 is required for synthesis. The syn-gas is produced in aratio of 1 carbon monoxide molecule (CO) for each hydrogen molecule (H₂)which represents a 50:50 ratio, however most preferably the synthesisgas having a ratio of 55:45 or 1:0.82 is required for the preferredsynthesis to occur. Gases rich in hydrogen can also be used, howeverhydrogen causes a shift in the composition of the product with aproportional increase in the ratio of hydrocarbons which are volatile atlower temperatures including the C₃ and C₄ hydrocarbons. The ratio of COto H₂ can be modified by replacing a proportion of steam used inproduction of syn-gas as will be described below with carbon dioxide.The gasification medium will most preferably comprise 27% by volume ofcarbon dioxide and 73% by volume of superheated steam which will attaina ratio of carbon monoxide to hydrogen of 55:45 or of 1:0.82. Thesyn-gas will be composed of 12.7% carbon dioxide, 47.7% carbon monoxide,39% H₂ with a minor remaining percentage (0.2%) of methane (CH₄) withthe balance being ash. The synthesis gas specified above is mostpreferably passed through a scrubbing process which will remove CO₂ andmethane. The process may also produce organic sulfur which can beremoved and stored suitably prior to sale as commodity sulfur. Thepurpose of the equipment is to produce synthetic diesel. The desirablesynthetic diesels produced has a density of about 850 g/liter (gasolinedensity equals about 720 g/liter or 15% less than diesel when convertedto heat by burning, typically diesel delivers about 41 megajoules (MJ)per liter which is substantially greater than gasoline (US—gas; Britain,and Australia—petrol) which produces less than 35 MJ/liter which is alsoabout 15% less than is derived from diesel. Production of diesel isgenerally simpler to refine than gasoline and should cost lessaccordingly. Most preferably the diesel produced in this process willhave a high cetane number and low to no sulfur content which normallywill be atypical property of diesel produced in the process describedherein. Higher cetane or carbon content synthetic diesel is preferredsuch as C₁₅H₃₂ which can be preferentially produced when thecorresponding catalyst(s) such as a cobalt based catalyst, is provided.The biomass used in the process described in association with FIG. 1 forthe production of syn-gas may include a wide range of substantiallywaste items such as the bark of trees, sawdust, any plant matter (hempor straw). It can also be produced from grain such as wheat, barley,corn, or from food scraps, garbage (for example, discarded cardboard andwaste paper products) and sewage sludge however, in all cases conversionof these materials to carbon by sufficient heat application, can all beused to produce synthesis gas (Syn-gas) which after purification andappropriate carbon to hydrogen ratio adjustment, used as the feedstockfluids in the Fischer-Tropsch process to produce synthetic diesel andeven polypropylene, for example, by way of subsequent processing ofnaphtha produced in the Fischer-Tropsch equipment. The process ofsynthesis gas production is typically referred to as biomass to liquid(BTL) and the syn-gas is then converted to synthetic diesel (a paraffinlike liquid) which can then be isomerized to provide stability prior todistillation which allows adjustment or “fine tuning” of the fuel tomatch the requirements of engines where the liquid produced is consumedas fuel. About 60% of the distillate can be used directly as diesel fuelwith the balance (40%) used in the plastics industry for example by wayof naphtha production or alternatively further processed into keroseneor jet engine fuel.

Referring again to FIG. 1 a hopper 55 enclosing space 3 narrowing to aconduit 56 which connects directly to a compression device is filledwith biomass in the direction shown by arrows 52. Space 3 is mostpreferably filled to a level greater than 75% or more specifically toprovide a dense but permeable mass into which can be injected oxygendisplacing gases such as carbon dioxide, nitrogen, or super heatedsteam. Such gases or fluids can be injected directly into conduit 56such that atmospheric oxygen will be displaced in the opposite directionafter traveling through the permeable biomass within hopper 55 in theopposite direction of arrows 52. This will result in a substantiallyoxygen free flow of biomass through conduit 56 and into the horizontalconduit 57 enclosing a compressing screw 5 driven by drive motor 4 suchthat the progressively compressed biomass is transferred in thedirection shown by arrow 6. Electrically or alternatively oil heatedband is tightly wound around conduit 57 and superheated steam isinjected at high pressure through conduits connecting directly with thehorizontal screw enclosing conduit 57 and in such a way that the biomasstransferred by Archimedes screw 5 will be substantially carbonized. Aconnecting conduit 9 tapering to provide a cone profile with the top andbase cut therefrom such that the small end of said cone is attached topressure vessel 58 containing space 59 such that the carbonized biomasswill explode into space 59 with solids dropping to the base of pressurevessel 58 in the opposite direction of arrow 19 and any gases containedtherein will travel upward through space 59 in the direction shown byarrow 19 passing through conduit 21 and into space 22 of condenser 26.The condenser comprises a heat exchanger enclosed within the pressurevessel 26 wherein a fluid maintained at a lower temperature istransferred via connecting conduits in the direction shown by arrow 20through the heat exchanger 25 and then there from via conduit 24 in thedirection shown by arrow 23. A space 27 is provided to enable theaccumulation of liquids within a portion of pressure vessel 26 prior totransfer via conduit 29 in the direction shown by arrow 28. The liquidmay comprise substantially water which is held within space 27 andconduit 29 and prevented from transfer via conduit 31 by a 3 way valve32 until the fluid is required to be re-blended with carbon in space 33of high speed blender 34. The solid carbon is again treated to ensurecomplete carbonizing and dehydration by transfer through screw 18enclosing conduit 60 in the direction shown by arrow 17. It is importantthat the carbonized biomass which comprises generally 100% friablecarbon after processing thus far is not greater than about between 2 and5 microns in diameter or maximum dimension across the widest distancefor each particle. The importance of this requirement will be describedherein below. Most preferably the carbon particle size will not exceed 5microns. This is achieved by transferring the dry heated friable carboninto space 33 enclosed by vessel 34 and with a high speed impellor 35mounted in the base of a circular cross section pressure vessel 34. Allenclosed vessels in the process described in association with FIG. 1must be capable of withstanding pressures in the order of 200 bar whichis about 3,000 pounds per square inch (psi). The rotating blade 35rotates up to 4,000 rpm and is provided with a carbide tip to each ofthe profiled blades at the extreme end away from the center point oraxis about which the blades rotate. The mixing blades may exceed a speedat the tip of 7,000 feet per minute and the temperature of the tipbecomes exceptionally high due to friction hence carbide tips arepreferable. The high velocity of the impellor 35 results in the smashingof carbon particles which due to its hot dry condition is predisposed tocrumbling and breaking down, however a ball mill can also provide asuitable means of reducing maximum particle size as required to not morethan 10 microns wherein large steel balls mixed with smaller steel ballsare blended with, the, in this instance, hot dry carbon (maintained at aselected temperature of between about 200° C. and up to 400° C.). Apreferred method is to install a high speed rotating impellor driven bya suitably sized electric motor 37 coupled directly to the drive shaft36 of the ball bearing mounted shaft coupled rigidly and perpendicularto mixing and grinding blades 35 mounted at the base of pressure vessel34. After reducing the maximum particle size in a given batch which maybe in the order of 3,000-5,000 lbs per batch contained withinapproximately one third of space 33, a fluid comprising condensed steam(water) and glycerol containing condensed gases and other fluids removedfrom the flow of biomass into space 59 of high pressure vessel 58 can betransferred through conduit 31 in a suitable controlled flow deliveringa precisely measured quantity and blended with the pulverized carbon toproduce a black liquid ready for further processing. FIG. 1 shows asingle high speed blender 34 however most preferably multiple blendersare arranged in such a fashion to allow the systematic use of a firstblender then a second blender followed by a third blender and so on,such that a continuous stream transferred from conduit 60 in thedirection shown by arrow 17 can be accommodated by the transfercontinuously and progressively into the high speed blender pressurevessels. Preferably a first high speed blender pressure vessel is beingfilled while a second vessel having similar capacities to said firstblender is in process and a third blender is unloading the processedcontents into conduit 81. Any number of blenders may be arranged so asto accommodate the continuous flow from conduit 60 diverted by way of asuitable multiple way valve to said first, second and third high speedblenders, thereby enabling a continuous stream into space 81 of conduit38 continuously to provide a stream of equal mass flow to the mass flowof conduit 60 transferred in the direction shown by arrow 17 combinedwith the flow of material in the direction as shown by arrow 19 plusadditional fluid such as glycerol which may be provided in a controlledstream via conduit 90 flowing in the direction shown by arrow 91 andinto space 27 of condenser enclosing pressure vessel 26. The purpose ofsubstantially filling vessel 26 with glycerol is to provide a means ofcollecting very fine solids and condensed gases including tar whileallowing steam to pass through. Steam may be allowed to escape via apressure regulated extraction port and into water condensing equipment(not shown) thereby enabling the recycling of water for use inproduction of super heated steam as required in the process. All matterother than condensed steam (i.e. water) with a quantity of glycerol istransferred via conduits 28 and 31 into space 33 and therein combinedwith carbon particles having been reduced in size to less than 4 micronsand as low as less than 1 micron across. Additional glycerol or anyliquid fuel such as diesel, even synthetic diesel produced in theprocess described herein below, can be transferred in controlledquantities via conduit 86 in the direction shown by arrow 88 and blendedwith the contents therein so as to produce a liquid or carbon particlesuspension having a controlled and specified viscosity suitable for theprocessing thereof by first compressing after transfer through space 81in manifold connecting space 33 thereto via a gate valve 80 which can beopened and closed to, when open allow transfer of said fluid into space81 in a controlled mass flow. Space 33 may also be pressurized by theinjection of carbon dioxide or alternatively syn-gas produced in thisprocess so as to eliminate the presence of air or oxygen. However acontrolled pressure in space 33 can enable the consistent transfer andmass flow of said fluid through gate valve 80 wherein an aperture isprovided having a controlled size of opening with the adjustment of gatevalve 80 by opening or closing the gate member in the directions shownby arrow 90. When vessel 34 is substantially empty gate valve 80 isclosed and the process repeated wherein carbon pieces are transferredinto space 33 in the direction shown by arrow 17 by the rotation ofscrew 18 within conduit 60. Member 35 comprises a two or other multiplebladed impellor having a profile most suited to the crushing of thefriable carbon pieces transferred into space 33. The electric motor 37which drives impellors 35 via a direct coupling 36 can also be used totransfer fluid from space 33 into manifold 81 and subsequently conduit38. When vessel 34 has been substantially emptied second and third andeven fourth and fifth or more vessels similar to 34 and also connectedto manifold 81 and therefore conduit 38 are progressively emptied onevessel at a time. The equipment is arranged such that the duplication ofhopper 55 with all other equipment as required to produce an equivalentamount ground matter through to manifold 81 duplicated for eachadditional vessel similar to vessel 34 is provided such that acontinuous and constant mass flow of fluid, comprising said carbonsuspension, is transferred to high pressure pump 40 via conduit 38. Thehigh pressure pump 40 has the capacity to elevate the pressure of saidfluid up to as much as 3000 psi or more or less and transfer thepressurized fluid into space 92 of conduit 43. During this sequence ofthe entire operation the fluid transferred into space 92 of conduit 43is heated to maintain a temperature which is progressively increased asthe fluid having been produced in space 33 and transferred to commonrail (conduit 43) around which is provided heating jacket 42 whichelevates the temperature of the fluid up to 1000 degrees C. or even moreand as much as 2000 degrees C. and at such a temperature which willcompensate for a reduction in temperature when transferred into space49. Common rail 43 branches into multiple, smaller diameter, highpressure conduits such as 47, 44 or 45. At the end of each high pressureconduit is provided a nozzle which comprises a relatively small diameterorifice which is adjustable in size to provide for the atomizing of saidfluid when sprayed under high pressure into space 49. Space 49 isenclosed with a cyclone comprising a cone shaped member 48 with the bigend of the cone completely enclosed by an assembly of high pressureinjectors, for example 47 and 46, and a suitably profiled member 94around which is provided a volute 96 having conduit 98 connected to asuitable supply of super heated steam. The volute which includes acircular profiled conduit at 96 gradually changing in cross sectionalprofile to a longer and narrower slot 46 wrapping around said member 94and connecting with a slot in the outer side of the upper end of cyclone48 and through which super heated steam is injected at a temperature ofat least 1000 degrees C. and injected into space 49 in a manner thatwill tend to cause the steam and the contents of cyclone 48 to spin ineither an anti-clockwise or clockwise direction but as shown in FIG. 1the direction will be in an anti-clockwise direction and at highvelocity. A quantity of steam proportionate with the fluid transferredthrough said injectors that inject said fluid into space 49 may betransferred into conduit 92 in such a manner to blend it with thecontents therein prior to the combined injection of said super heatedsteam and fluid into space 49. The super heated steam transferred viaconduit 98 and subsequently 46 and also with the fluid transferred viaconduits 44, 45, etcetera, must be at least of sufficient volume,pressure, and temperature, to react with the suspended carbon particlestransferred into space 49. The contents of said fluid injected therein,having originated from vessel 34, comprises substantially all carbonparticles. In fact the temperature maintained within space 33 of vessel34 must be of a high enough value to cause any organic matter such asthe glycerol and its content provided therein, into carbon. Thetemperature within cyclone 48 and all conduits connected therewith, andthrough which fluid is transferred into cyclone 48, must be maintainedat a temperature that will carbonize the contents therein enclosed.Steam injected into conduit 92 blends with the carbon particles andcarries them into cyclone 48 by which time the particles of carbon willhave reacted with the super heated steam to produce what is commonlyknown as syn-gas which comprises in this instance, an equal quantity ofcarbon monoxide mols and hydrogen mols. Even steam transferred viavolute 46 will have substantially reacted with the particles transferredinto cyclone member 48. The nozzles or injectors provided at the end ofeach high pressure conduit 44, 45, 46, and 47 etcetera, can be arrangedto open and close rapidly so as to enable spurts of steam and suspendedcarbon particles, and in such a manner that will result in the relativevelocity of said carbon particles suspended in the super heated steamversus said super heated steam to vary and in so varying, causing areaction that is taking place between the carbon particles and the steamto be enhanced. The endothermic reaction between said carbon particlesand said super heated steam varies according to the reactants madeavailable such as shown in the following examples:

Heat+H₂O+C→CO+H₂

And subsequent to production of carbon monoxide, to a minor andcontrolled extent;

Heat+H₂O+CO→CO₂+H₂

A single molecule of each carbon monoxide and hydrogen are produced froma single molecule of super heated steam (preferably to 1,000° C. ormore) and one carbon atom; this reaction can most preferably becontrolled by providing heat in the form of electricity discharged viaan element made from a suitable material such as Tungsten held in aposition by an insulating material (such as Al₂O₃), or series ofelements arranged to enclose the vessel or cyclone 48 as shown in FIG.1; said elements being held in close proximity to the vessels while notcontacting the vessels. Insulation can enclose the cyclone completelyover all external surfaces with the electrical heating elements locatedbetween the insulation comprising an outermost layer and the cyclone (orother suitable pressure vessel) located on the inner side of the heatingelements. The electrical heating elements are most preferably held inclose proximity to the vessels, around which they are located but not incontact with the outer surface of the cyclone (or other vessel) and theinsulation is located in a layer of adequate thickness over the entireouter surface thereby enclosing the heating elements between insulationand the outer surface of the cyclone in such a manner so as to allowheating of the cyclone or other vessels by radiation means only. In thisway locating the heat source as close as possible to the inner surfaceof the cyclone with which the carbon and steam are in intimate contactdue to the rotating action of the fluids (gases) and carbon particlesbeing transferred through the cyclone. In this way the reaction betweenthe reactants can occur with the least disruption due to gases producedand emanating from the surface of the carbon particles after the steamreacts with carbon at the outer surface of the carbon particles. Takenote that the super heated steam can be prevented from contacting thecarbon particle surface by the hydrogen and carbon monoxide gases whichare formed when the super heated steam comes into contact with thecarbon. By locating the electric heating elements adjacent to the outermetal surface of the cyclone and in close proximity but not in contacttherewith, heat is transferred to the metal walls by intense heatradiation and through the metal walls of the cyclone which can thenprovide the heat required to facilitate the reaction(s) responsible forproducing the syn-gas, which may, in another preferred embodiment, be asset out below;

Heat+H₂O+C→CO+H₂

Or alternatively and most preferably carbon dioxide can be added to thesuper heated steam in controlled relative proportions to yield syn-gascomprising hydrogen and carbon monoxide as follows;

Heat+H₂O+2CO₂+3C₅CO+H₂

Other reactions, such as the following, can occur;

Heat+H₂O+CO→CO₂+H₂

However, the catalysts used in the subsequent reaction vessels can bearranged such that only desired reactions are either inhibited orenhanced, so as to result in production of a syn-gas comprisingpredominantly hydrogen and carbon monoxide in only those relativeproportions as may be desired, with a proportion of carbon dioxide ifrequired; therefore, by catalytic control, the various reactions can becontrolled so as to produce a syn-gas comprising the desired proportionsof hydrogen and carbon monoxide and if any undesirable carbon dioxideand/or steam/water vapor are present the syn-gas can be “scrubbed” withclean water and then cooled and dried prior to transferring into thefinal reaction vessel within which the syn-gas is converted to dieseland other matter such as naphtha.

The above reaction (line 0039) is considered to be very important sinceany carbon dioxide such as that produced in massive quantities by thenumerous coal fired electricity generating plants often located at thecoal or lignite sources around the world. Natural gas can also be usedto generate electricity and any CO₂ produced by burning the natural gas(or coal) can be, essentially, re-cycled instead of being dumped intothe atmosphere. This re-use of CO₂ in fact is facilitating theproduction of liquid fuels from the syn-gas which in turn was producedby applying energy in the form of electricity to produce heat needed inthe endothermic reaction. Therefore, the electricity is in factconverted into liquid fuel and this method therefore provides a veryefficient process in which all carbon dioxide generated by the burningof fossil fuels to generate much needed electrical power for industryand domestic purposes can be re-cycled and retained by the liquid fueluntil use. Given the high volume of fossil fuels used in diesel and gasengines the above reaction can have the effect of reducing the amount offossil fuel needed by at least 40% to 50%.

In another preferred embodiment, electricity generated by windmill ormore specifically, wind generated electricity and/or hydroelectricityand/or electrical power generated by way of wave action or tidalmovement can be used to convert CO₂ into liquid fuel such as diesel,thereby displacing the need for producing a corresponding volume ofliquid fossil fuels. Electricity, discharged via suitable heatingelements to provide the heat required to generate super heated steam andotherwise or additionally heating of the vessels within which thesyn-gas is produced, is most preferably generated by wind turbine andtransferred to the equipment which is most preferably located adjacentto the wind turbine or within a distance such that any electricalconnecting cable electrical power “line loss” is insignificant.

Heat+H₂O+CO→CO₂+H₂

In another preferred embodiment the ratio of hydrogen to carbon monoxidein syn-gas required for production of a particular product such asplastics, ethanol, or any liquid fuel by Fischer-Tropsch methods can beproduced in a similar manner to the production process disclosed abovefor fossil fuels. The three Reactions (A), (B) and (C) below, whereinthe reactions (A) and (B) represents the production of syn-gas in anyreactor intended for production of syn-gas disclosed herein and whereReaction (C) may be the electrolysis of water by the Hoffman processwhich can produce a first isolated gas of hydrogen gas and a secondisolated gas of oxygen. By adding a measured quantity of the hydrogengas to a syn-gas requiring more hydrogen or alternatively adding thesyn-gas of Reaction (B) which contains more carbon monoxide, to thesyn-gas requiring more carbon monoxide any blend of syn-gas can beprepared prior to transferring into the Fischer—Tropsch reactors (asdisclosed herein);

Electric Heat+H₂0+C→H₂+CO  Reaction (A)

Electric Heat+H₂0+2CO₂+3C→H₂+5CO  Reaction (B)

Electricity+2H₂0→2H₂+O₂  Reaction (C)

Super heated steam is aggressively corrosive, particularly at highertemperatures (above 600° C.) such as is required to achieve the abovereaction as occurs with steam “reforming” and the correspondingproduction of carbon monoxide and hydrogen from water and carbon. Thereaction is enhanced when the exposed surface area of carbon to superheated steam is increased and therefore the reduction of the carbonparticle size enhances the reaction. Most preferably the carbon particlesize should be reduced to about 30 microns (wherein 1 mm=1,000 microns)are small and the super heated steam has a temperature in excess of 600°C. and <1000° C. The present equipment provides for these requirements,most preferably with electric heating providing overwhelming radiatedheat and in the arrangement illustrated in FIG. 1, the volute with inlet98 which provides an inlet wherein the cross sectional profileprogressively changes profile from a circular (round) cross section ofthe conduit 96 to an elongated aperture with short horizontal sides andlonger parallel vertical sides at 46 which become closer together as thevolute extends around the upper, circular section of the cyclone 48,connecting with a narrow slot communicating at a tangential dispositiondirectly with the space 49 of the cyclone 48. The sides of said voluteare heated by way of electric discharge thereby providing overwhelmingheat by way of radiation for the entire member 94. The conduits such as45 and 44 are heated in a similar fashion and the above reaction isalready occurring within the enclosed pressurized conduits even beforerelease by injection into space 49. The adequate supply of super heatedsteam in sufficient quantities to provide at least sufficient hydrogenand oxygen ions needed to complete the gasification of the entirequantity of carbon transferred in the pressurized streams withinconduits such as 44 and 45. Therefore excessive quantities of superheated steam must be provided. Additionally the super heated steammaintained at a temperature of 800 degrees C. or more and mostpreferably 1000 degrees C., enters the upper region of space 49 at highvelocity through the volute which includes the inlet at aperture 98which wraps around the upper section of cyclone 48 in a circulardirection with slot 46 communicating with said space 49 via unseensection of volute which has been cutaway for ease of representation andclear description of the process. The high velocity and mass flow whenentering through the narrow slot communicating with the inner space ofsaid cyclone, results in a rotation of the entire contents of saidcyclone 48 at a velocity that causes any remaining carbon particles as aresult of centrifugal forces, becoming carried by the rotating superheated steam around the inner wall of said cyclone 48. The super heatedsteam therefore carries the carbon particles in a direction whichrotates around the inner cyclone wall anti-clockwise but also steadilyfalling toward the extraction port connecting with extruder having drivemotor 50 and enclosing screw 51 in a gas tight sealed connectioncommunicating between space 49 and enclosed screw 51 and generally inthe direction shown by arrow 150. The remaining carbon particles if anydo remain, are carried by said stream of super heated steam around theconical profiled inner perimeter of the inner face of cyclone 48. Therotating action causes the heaviest solids to a close and contactingproximity to the inner contour of the conical cyclone while movingsteadily downward in the direction shown by arrow 150. The typicalcyclonic action common with all cyclones operated correctly results inthe gradually descending solids traveling at an ever increasing velocitywhich results from the reducing diameter of the circular direction ofthe super heated steam driven particles of carbon and ash. The reactionbetween superheated steam and carbon results in gaseous carbon monoxideand hydrogen emanating outward away from a point of reaction at theouter face of all carbon particles that remain. This reaction requiresan aggressive mixing action in addition to abundant super heated steambecause the emanating gas prevents the steam from contacting the surfaceof the carbon by the inherent insulating effect that the two gasesprovide, so in order to ensure that a reaction occurs the removal of thetwo gases from the outer surface of each carbon particle is essential.More specifically the reaction with super heated steam, which results inproduction of carbon monoxide and hydrogen at the exact location wheresuper heated steam must be present for the reaction to continue.Clearly, the gas has the capacity to prevent the reaction from occurringby its inherent direction of flow outward and away from the carbonparticle responsible for its production in combination with said superheated steam. To achieve the preferred conditions and enhance thedesired reaction, most preferably the velocity of said steam streamsmust be substantially greater and most preferably in a differentdirection to those of the carbon particles. Such preferred conditionsare provided by the action within the typical cyclone when arranged asdisclosed herein above and wherein the injection which can be arrangedin an intermittent manner into space 49 similar to that of a Piezoinjector providing many opening and closing actions within a singlesecond, collides with the tangential direction of an overwhelming streamof suitably heated super heated steam which immediately blasts thesurfaces of any remaining carbon particles attracted to the stream wheresuch attraction is overwhelming due to an enclosed confined space 49 andthe conical profile of said cyclone 48. The inner surface of cyclone 48is also heated by electric band heaters that cover the external surfaceof the cyclone while the centrifugal force causes the heavier carbonparticles to contact the inner surface of the cyclone walls, therebyremaining in close proximity to the radiated heat required for thereaction in combination with super heated steam, all of which acceleratearound the inner perimeter. The injection, blasting force of said streamof super heated steam, followed by the acceleration and close proximityto the source of radiated heat all combine and conspire to provide theconditions required to overcome the barrier effect of gases producedresulting in the thorough and rapid conversion to gases of saidparticles and any ash that remains after gasification reaction iscarried firstly in the direction of arrow 150 into the spaces betweenthe spiraling screw depressions of screw 51 rotating and carrying solidash toward the constricted space of 151 immediately downstream from theextraction end of screw 51. The enclosure 152 of screw 51 is in directcommunication with cyclone 48 via port 153 providing one of only twocommunications directly with exit ports of space 49. The arrangementshown provides a means of extracting solids while retaining the highpressure required within space 49 which is achieved by severalpurposeful arrangements and the first of these is provided by thecompaction of ash within space 151 which is also of conical profile soas to provide for the compaction of ash thereby restricting the escapeof high pressure gases in space 49. Fluid can be provided throughconduits 52 and 54 in the direction shown by arrows 53 and 55 whereinthe fluid injected comprises any suitable liquid such as water withadhesive provided in a manner that will blend with ash resulting in aheavy compacted plug of ask material that is forced through constrictingspace 151 in the direction shown by arrow 56 and into an enclosed vessel(not shown) that is totally sealed and only emptied either when theequipment is not in use or a valve provided at the down streamconnection of member 152, connecting with said pressurized vessel.Multiple such vessels can be provided. Syn-gas produced is transferredvia the open end 102 of conduit 100 and the exit pressure thereof iscontrolled by pump 11.

Biomass such as municipal garbage may be transferred into the equipmentshown in FIG. 1 and in the direction of arrow 52, after granulating topulverize carbon in granulator 110 arranged to reduce particle sizes ofany matter transferred therein in the direction of arrow 111 and therefrom via conduit 113 in the direction shown by arrow 112 immediatelyprior to transfer into hopper 55 in the direction shown by arrows 52.

During the processing of any organic matter such as biomass andmunicipal garbage within the closed barrel extruder (other than inlet 8into which super heated steam is transferred) virtually pure solidcarbon residue is produced with the balance of all other mattertypically converted into steam (from water), and various gaseousvolatiles. In FIG. 1 all solids transferred through hopper 3 and intothe barrel 57 of extruder driven by drive motor 4, are transferred inthe direction shown by arrow 6 and heated by band heater method means tosuch a temperature that the solids are terrified or carbonized. Theprocess divides all organic matter into carbon with a crumbly andfriable texture and which is transferred within chamber 58 downward andalong barrel 60 in the direction shown by arrow 17. All other steam andgaseous matter is transferred upward in the direction shown by arrow 19and into space 22 via conduit 21 wherein the gas and steam can bedissolved into glycerol or condensed and mixed with glycerol and anyother suitable matter such as water within space 27. Refrigeration isprovided to heat exchanger 25 with the refrigerant being transferredthere from via conduit 24 in the direction shown by arrow 23. Thisprocess divides all matter transferred via hopper 3 into two streams.The first stream comprising substantially pure carbon and a secondgaseous stream subsequently liquefied by condensing and/or blending withglycerol. In one preferred embodiment. Said first and second streams canbe processed by recombining as disclosed herein within high speedblender space 33. However alternatively said first and second streamscan be processed via two entirely separate streams by treatment withinduplicated equipment disclosed herein in association with FIG. 8, FIG.9, FIG. 8 (i), and FIG. 9 (i) whereby said first stream of pulverizedcarbon can be treated by blending with a measured quantity of water orsuper heated steam in which case a more complete reaction producingsubstantially only carbon monoxide, hydrogen and carbon dioxide in smallquantities and said second stream, treated separately, via similarequipment wherein a greater quantity of carbon dioxide is likely to beproduced and therefore retained within syn-gas thereby produced. Suchsyn-gas can then be, if so desired, treated by separation of hydrogenand carbon monoxide with use of membrane separation equipment such asmaybe provided by many corporations dealing with membrane separationtechnologies including Alfa Laval Nakskov A.S., Denmark; DonaldsonMembranes, Newton Le Willows, England; and, Euroby Limited, Worthing,Sussex, UK. The membrane separation process can provide a means ofseparating and isolating a selected gas which may be, for example,hydrogen gas. Hydrogen gas may then be combined with other syn-gasstreams to provide a syn-gas comprising larger ratio of hydrogen such asapproximately two thirds hydrogen with the remaining one thirdcomprising carbon monoxide; or, alternatively by separating a stream ofcarbon monoxide for combination with a stream of syn-gas to yield asyn-gas stream of two thirds carbon monoxide and one third hydrogen.

Such isolated continuous streams of syn-gas, comprising a “trimmed”composition of selected CO:H₂ proportions (e.g. 55% CO:H₂ 45%) aresuitable for predominantly diesel fuel production by transferring thestream of syn-gas to a Fischer synthesis reactor maintained at atemperature range between 200 to 250 degrees C. containing a catalystincluding cobalt, so as to yield a greater percentage of diesel oil.

Most preferably the source of energy to heat the equipment and drive theelectric motors all shown. The reaction is catalyzed by metals such asnickel, tungsten, ruthenium and molybdenum in connection with FIG. 1will be sourced from wind generators or hydro-electric sources.Alternatively, electric generators driven by wind, will be installedwith each facility and arranged to provide power in such a way that atleast the amount of electric power required in total will be produced bythe wind powered generators. This may require the sale of surplus windgenerated power to regional utilities.

The gas produced comprising hydrogen and carbon monoxide with some watervapor is transferred through the open end of conduit 100 at 102 in thedirection shown by arrow 104 and arrows 106 and 108, along conduit 110and directly to the inlet of gas pump 11. Gas comprising substantiallyan equal quantity each of hydrogen and carbon monoxide is thereforetransferred in the direction shown by arrow 10 via conduit 112.

Referring now to FIG. 1( i) a cross section through an equipmentdesigned to provide a method of continuous renewable fuel productionfrom triglycerides derived from either animal or plant origin is shown.The equipment is comprised of an outer cylindrical member 904 enclosinga series of machined discs such as 932 and 931 fixed rigidly to acentrally disposed driveshaft 925 with centerline 933 and interposeddiscs such as 929 and 912 machined so as to provide a barrier betweensaid first temperature-controlling stream and a second stream followinga second pathway flowing in the direction shown by arrows 860, 702, 864and 700 in the opposing direction to said first temperature-controllingstream. Said first temperature-controlling stream is further restrictedby discs such as 800, 802, 804, 806, 808 and 810 wherein the outer rimof each disc is attached rigidly and sealingly to tubular sections heldwithin outer cylinder 904 and in direct contact therewith at interface905. Each cylindrical segment such as 1000 is attached to a disc membersimilar to 803 at the outer perimeter of the disc member and the innersurface of a cylindrical member such as 1000.

The annular point of contact such as 800 between each disc member suchas 803 with each tubular member such as 1000 can be sealed by welding(as shown in FIG. 1( iii), items 7000 and 7001) in place and arrangedsuch that an enclosed pathway such as 807 allowing said firsttemperature-controlling stream to flow as shown by arrow 890 and on theopposing side of disc 803 pathway 815 in the direction shown by arrow805 with annular space 862 connecting both sides of disc 803 around theinner edge thereof. In this way a continuous stream oftemperature-controlling fluid such as and most preferably glycerol canbe injected into an annular port represented by arrow 1010 so as to flowin the direction shown by arrow 816 along a radial pathway extendingoutwardly and away from centerline 933 communicating directly with aperpendicular pathway 1002 which communicates directly with a radialpathway following an outer surface of disc member 810 in the directionshown by arrow 811 through annular space 814 connecting with pathway1003 flowing in an outward radial direction represented by arrow 809communicating directly with the next perpendicular pathway and so on.Members 1005 and 1004 are machined most preferably a suitable steelmaterial such as inconel and located adjacent to rotating disc 1006providing a space of between 100 microns and 200 microns at theinterface 1007 between member 1005 and disc member 1006 and interface1008 between member 1004 and disc 1006. An annular space 812 istherefore enclosed by members 1005 and 1004 and rotating disc member1006 with contact between members 1005 and 1004 at contact point 1009.The contact point 1009 extends the full distance around a perimeter ofeach member 1004 and 1005 and when said members 1004 and 1005 are infull contact with each other around the perimeter at 1009 with allmembers such as 1004 and 1005 held together by clamping forcerepresented by arrow 928 with opposing arrow 927 and of such magnitudeso as to ensure that each pair of rotating discs enclosing members suchas 1004 and 1005 are in contact with each other thereby providing a sealpreventing any fluid that may be in space 812 or space 796 or space 832cannot escape from spaces such as 812 outward between members 1004 and1005 and into perpendicular channel such as 1002. “0” rings such as 822and 888 are provided between each pair of members such as 1004 and 1005to seal the annular contact point between each adjacent pair of memberssuch as 1004 and 1005. Clamping force 927 and 928 as can be seen areopposing and provided so as to ensure all members discs stacked betweeneach end are held together with a space of approximately 100 microns to200 microns between each rotating disc such as 1006 and the adjacentpair of enclosing members such as 1004 and 1005. In this way said secondpathway through which fluids can be transferred in the direction such asarrow 702 into annular space 832 and therefrom as shown by arrow 700between rotating disc 932 and adjacent enclosing member 1012 and intoperpendicular space 1013 in the direction shown by arrow 1014 then alongspace between member 1015 and rotating disc 931 in the direction shownby arrow 1016 and so on. In this way triglycerides represented by arrow936, supercritical carbon dioxide shown by arrow 938, and ethanolrepresented by arrow 930 can be injected in a continuous stream intoannular space 922 in which is provided a series of spaces created by aseries of vertically disposed metallic separators spaced atapproximately 1 mm distance between a first and a second space-definingmetallic separator. Said radially disposed space-separating metallicmembers are fixed to member 925 such that when member 925 is rotated ameasured quantity of each of fluids represented by arrows 936, 938 and940 is injected into each space. Said fluids comprising triglycerides,carbon dioxide and ethanol are injected under high pressure such asbetween 2,000 psi and 3,000 psi but most preferably 2,500 psi andproportioned relative to each other according to measured proportionsprovided in a continuous flow wherein each fluid is pumped separately bya suitable pump such as positive displacement diaphragm pumps such as ismanufactured by Bran & Luebbe. Said radially disposed annular spaces 930provide an intensive mixing mechanism as shown in FIG. 1( ii). Saidintensive mixing mechanism comprises spaces as shown in FIG. 1 (ii)having direct close contacting disposition relative to each port throughwhich the triglyceride, ethanol and supercritical carbon dioxide fluidsare transferred wherein said ports are static and annular space 930rotating at approximately 28,000 rpm or less or more. The intensiveblending action provided to the triglycerides, ethanol and carbondioxide at 922 occurs immediately prior to transfer of the blendedfluids through space 924 and into interface 798 in the direction shownby arrow 760. The enclosing members such as 1015 may be held fixedrelative to outer cylinder 904 while central driveshaft 925 withattached rotating disc such as 1006 and 931 or 932 rotate atapproximately 28,000 rpm. Alternatively members such as 1015 may berotated in the opposite direction to discs 932 and 931 etc however mostimportantly the differential between the rotating speed of members 932and 931 and enclosing such as 1015 and 1012 is approximately 28,000 rpm.In this way a high shear is subjected to the fluid transferred in thedirection shown by arrows 702 and 860. In normal operation an electricdrive motor is attached to shaft 925 in such a way that vibration willnot affect the operation thereof.

Referring now to FIG. 1( iii) and Area “A” of FIG. 1( i) fr5 as shown inFIG. 1 (iii) is defined by three straight broken lines in FIG. 1 (i) butin an enlarged view. In this way the flow of fluids through theequipment as shown in FIG. 1 (i) can more clearly be understood.Centerline 933 of shaft 925 as shown in FIG. 1 (i) is numbered likewisein FIG. 1 (iii) and barrier discs 806 and 804 are also commonlyindicated in both FIG. 1 (i) and FIG. 1 (iii). Thetemperature-controlling fluid referenced in FIG. 1 (i) flows in thedirection shown by arrow 200 through conduit 201. Outer cylinder 904 isshown by the same number in FIG. 1 (i) and FIG. 1 (iii) and solid line905 shown in FIG. 1 (i) and FIG. 1 (iii) represents the interface wherethe inner surface of 904 and the outer surface of bushings 905. Bushing235 and bushing 221 are shown in position and adjacent to one anotherwith the contact face represented by solid line 227 in FIG. 1 (iii). Foreach barrier disc such as 806 and 804 as shown in FIG. 1 (iii) and allother barrier discs shown in FIG. 1 (i) such as 810, 808, and 800 theseparation between each bushing as shown by line 227 in FIG. 1 (iii) isparallel and on the same plain as the centerline of each disc such as247 in FIG. 1 (iii) however after assembly of the equipment the bushingare held tightly together by compression from the end of each bushingshown for example in FIG. 1 (i) by the solid lines 814 and 809 howeverpressure applied at each end of the equipment applied to hold each endof the members such as 248 and 211 as shown in FIG. 1 (iii) isindependently maintained and is adjustable by the variation of thehydraulic pressure through conduits 900 and 901 as shown in FIG. 1 (i).Said hydraulic pressure applied so as to retain said members 248 and 211together and in substantially parallel condition can be varied andadjusted so as to flow through said conduits 901 and 900 in thedirection shown by double-headed arrow 999 and 989 as shown in FIG. 1(i). Said hydraulic pressure may be applied and controlled via asuitable pressure regulator such as manufactured and distributed byParker Hydraulics and at a pressure of approximately 2,000 psi to 6,000psi. During operation of the equipment shown in FIG. 1 (i) saidtemperature-regulating fluid shown by arrow 200 in FIG. 1 (iii) andarrow 202 showing the direction of flow between barrier disc 806 andmember 209 may be any suitable fluid manufactured for the purpose ofheat transfer and temperature regulation however most preferably thefluid will be glycerol. Said fluid flows in the direction shown byarrows 202, 207, 213 is arranged to pass through annular opening 214 andthen in the direction shown by arrow 213 which opposes the direction ofarrow 207 therefore as can be readily understood saidtemperature-controlling glycerol fluid is in intimate contact withmembers such as 209, 211 and 248 as shown in FIG. 1 (iii) and able toabsorb heat hat may be generated by an exothermic reaction within forexample space 238 or in channels 210 and 252. Alternatively in the eventof an endothermic reaction occurring heat may be transferred from anexternal source to said members such as 248 and 211 and thereby whensaid fluid glycerol is transferred in said controlled manner thetemperature of said members 248 and 241 for example can be controlledwithin a narrow range of variation. Fluid reactants which may eithergaseous or liquid when subjected to normal atmospheric conditions can becompressed if said fluid is a gas to provide a dense vapor such assupercritical carbon dioxide or alternatively triglycerides which arenormally in liquid phase under atmospheric conditions can be pumpedtogether with for example ethanol or methanol in the direction shown byarrows 260 in annular channel 262 and subsequently through microchannel252 into space 238 or 215 and after passing in the direction shown byarrow 240 through microchannel 210 and then along channel 216 as shownin FIG. 1 (iii). When subjected to the appropriate pressure andtemperature such as about 3,000 psi or less or more and 270 C. or lessor more the reactants comprising triglycerides and ethanol will react toproduce bio-diesel otherwise known as fatty esters and glycerol. Thisreaction is clearly detailed in patent disclosures by the presentinventor and in patent disclosures filed at the USPTO by the presentinventor or his agents including the USPTO. Such a reaction is inhibitedby the presence of the glycerol that it produces and a purpose of theequipment disclosed herein is to provide a means of separating saidglycerol from the reacting stream such as when occurring in microchannel252 by means of a centrifugal separating force through aperture at 224.Members 211 and 348 are arranged such that aperture with centerlinerepresented by solid line 224 is normally closed and held in a tightclosed and sealed position by application of clamping force created whensufficiently pressurized hydraulic fluid is transferred into bothopposing ends of the equipment via conduit 900 and 989. Said aperturecan be opened by reducing hydraulic pressure applied at each end of theequipment through conduits 900 and 901 and also increasing the pressureof fluids in space 238 which is achieved by elevating the pressure offluids transferred via the three streams 936, 938 and 940. Opening saidaperture to allow the extraction of glycerol enables glycerol havingaccumulated in space 238 as a result of centrifugal force caused by therotation of shaft 925 about the axis 933 with sufficient speed to causethe accumulation in space 238 to pass in the direction shown by arrow245 through the aperture at 224 and into the channel 201 and uponclosing said aperture at 224 any flow of fluid therethrough is stopped.In this way after the accumulation of glycerol in space 238 the quantityof glycerol that remains accumulated in space 238 can be controlled byopening and then closing said aperture at 224. Said aperture at 224comprises an annular opening between the members such as 248 and 211about a centerline represented by 224 and said aperture can be openedand closed as required by adjusting the pressure of hydraulic fluidtransferred via conduits 900 and 901 and/or adjusting the pressurewithin space 238. Two parallel lines 245 and 206 are spaced apart toenclose a space 205 located between space 238 and space 215. Space 238comprises an annular ring enclosed within borders represented by theline 204, 203 and 237 whereas annular ring comprising space 215 has anouter perimeter represented by line 206. Space 205 is located betweenthe outer perimeter 206 of said inner space 215 and the inner perimeter204 of outer space 238. Glycerol can be accumulated progressively anduntil it fills the entire space comprising 205 and 238 and after therelease of a quantity of glycerol having a volume equal to the volume ofthe annular ring comprising the space defined by outer perimeter line204 and inner perimeter line 206 thereby reducing the quantity ofaccumulated glycerol to that contained within the space 238 having aninner perimeter line represented by line 204. The reaction between saidreactants transferred through space 262 in the direction shown by arrow260 continues progressively and the equipment is arranged to enable theseparation of glycerol from the reactants transferred via microchannel252 when occupying space 215. This is achieved because glycerol has aspecific gravity significantly greater than the reactants. Thereforeafter separation of glycerol cause by said centrifugal force wherebyglycerol is transferred in the direction shown by arrow 245 theremaining reactants are transferred in the direction shown by arrow 240and into microchannel 210 and then in the direction shown by arrow 241.The reaction between the reactants specified as triglycerides, ethanoland supercritical carbon dioxide is endothermic and it is thereforenecessary to provide sufficient heat to maintain the reaction. Howeverthe equipment disclosed herein in association with FIG. 1 (i) and FIG. 1(iii) can be modified by way of replacing spinning members for example247 with catalysts such as cobalt oxide having been crushed andcompacted into the space between the perimeters represented by lines 210and 252. The equipment when modified in this way can be used in aFischer-Tropsch synthesis production of synthetic diesel by compressingthe syn-gas trimming the ratio of hydrogen molecules to a desired ratiorelative to carbon monoxide (CO) and transferring the compressed syn-gasvapor through the annular space 262 as shown in FIG. 1 (iii) and intospace represented by 247 between the granules of cobalt oxide and anyliquid synthetic diesel produced as a result of the reaction. Themolecules of syn-gas will transfer in the direction shown by arrow 245and through annular space at 226 and into a stream of identical fluid inspace 201. Temperature of the equipment will be controlled by thetransfer of large quantities of diesel in the direction shown forexample by the arrow 200, 202, 207 and 213. The Fischer-Tropsch reactioncan be adjusted by changing temperature, prevailing pressure and thecatalyst used. However, in all cases the Fischer-Tropsch reaction isexothermic and will require the removal of excess heat and the equipmentdisclosed by FIG. 1 (i) and FIG. 1 (iii) is suitable for thisapplication and when the shaft 925 is rotated about the axis 933. At aselected speed fluids can be transferred from space 247 and into thechannel 201 with excess fluid being removed while retaining sufficientsynthetic diesel to provide an adequate temperature-controlling mediumby use of an external heat exchanger and refrigeration of adequatecapacity reducing the temperature of the recycled fluid.

Referring now to FIG. 2 a cross section of a segment of a dynamic microchannel equipment is shown. The cross section shown in FIG. 2 indiagrammatic format comprises an outer vessel illustrated by verticalsolid lines on the left hand side 18 and the right hand side 31, whichare representative of the two sides of a circular cross section pressurevessel mounted securely within said outer pressure vessel a secondpressure vessel represented by vertical lines 2 and 14 which areparallel with the outer walls of outer pressure vessel is also ofcircular cross sectional profile. Therefore if one was to look at theplan view of a vertically disposed pair of pressure vessels representedby the lines 18 and 31 with 2 and 14 located inward of the outer vessel,an outer circular vessel wall represented by 18 and 31 would be visiblewith an inner vessel securely fixed and having a gap 17 and 31 of equaldistance from the walls of pressure vessel represented by vertical lines2 and 14. At the center of the pressure vessels, a motor driven shaft 68would be seen as the inner most member of the equipment. Each end of thepressure vessels are enclosed most preferably by a hemispherical memberof suitable size such that the largest diameter peripheral edge of thecircular edge mates with a corresponding pressure vessel with a heavywall conduit 78 passing through both vessel hemispherical end caps andattached thereto rigidly at each end of the complete vessel. Thereforethe two vessels comprising the outer vessel represented in FIG. 2 bylines 18 and 31 and the second innermost pressure vessel represented bythe lines 14 and 2 are held relative to each other rigidly and in afixed position with a heavy walled conduit comprising a solid bar havingbeen bored out to allow a shaft shown as 68 with suitable bushings,seals, and bearings mounted centrally of the two pressure vessels. Atone end of the assembly described thus far in association with FIG. 2, aseal most preferably comprising a pair of bearing members 56 and 54having a space there between in which is contained a suitable fluidwhich comprises a component of the bearing assembly. At the end of shaft68 which passes directly through the sealed bearing of members 56 and 54is connected to a driving mechanism such as the hydraulic motor or anelectric motor which may include a reducer or any suitable gearmechanism which provides a means of turning central shaft 68 at a speedvariable as required. Three conduits represented by 7, 8, and 6 areprovided at the center of an end and comprising heavy walled highpressure pipe each communicate with annular space 80 and connect saidannular space 80 with three high pressure pumps or more or less but inany event in one instance, said three conduits 7, 6, and 8 are connecteddirectly with a single conduit, for example conduit 112 of FIG. 1. Theinner vessel represented by perimeter wall 2 and 14 is held centrallyand enclosed by space 17 and 31 which is filled with the pressurizedfluid such as carbon dioxide vapor, super heated steam, or super heatedwater, or chilled water as may be required, glycerol and mineral oil orsuitable oils of any kind, and in any event the temperature of vessel 2,14 is maintained as desired such as 200 degrees C. or more or less, butmost preferably at a temperature which will enhance the production ofliquids such as ethanol, gasoline, or diesel (C₁₀H₂₂), to (C₁₅H₃₂)ethylene (C₂H₄), paraffin (C₂₄H₅₂), olefin (C₁₀H₂₂), polypropylene(C₃H₆)n. The entire space within the outer vessel represented by 18 and31 is pressurized at substantially the same pressure however thepressure in spaces represented by 17 and 31 will be less than thepressure in annular space 80. The inner pressure vessel represented bythe lines 2 and 14 is attached to an internal assembly by way of fixeddiscs such as 3, 5, or 23, of circular profiled substantially the samecircle diameter as the inner diameter of the vessel represented by 2 and14. However for each disc a concentric round hole is provided to allowfirstly the inner channel through which fluids represented by arrows 42and 27 can be transferred wherein members 24, 34, 48, 50, and 26 whichare also circular discs, however having an inner aperture with a smallerdiameter than the diameter of aperture at the center of discs 3, 5, and23 etcetera. Sections of tube 84, 86, and 88, cut to the same length andof an outer diameter the same as the inner diameter of the concentricholes in discs such as 24, 34, 48, 50, 92, and 26 which are cut suchthat tube sections 84, 86, and 88, for example can be attached theretoby welding but in any event connected to said discs in a sealing mannersuch that no fluids can leak there through. At the outer perimeter ofdiscs 24, 34, 48, 50, 92, and 26, sections of tube such as 82, 90, and89, are attached and sealed thereto in such a manner that a channel 62,94, 96, 98, and 25, is created. In this way a fluid which is mostpreferably the same as fluid in space 17 can be transferred in thedirection shown by arrows 46, 60, 27, 40, 96, 1, and 44, and also arrows12, can be transferred in the direction shown. Said fluid transferredvia outer channels is temperature controlled such that if a reactiontaking place in an adjacent channel is endothermic then sufficient heatcan be provided via the fluid medium transferred through said outerchannels. However if the reaction occurring in an adjacent channel isexothermic then the fluid in said outer channels can be arranged tocarry the heat away and in both cases, whether endothermic orexothermic, the fluid transferred through said outer channels and alsocontained in pressurized space 17 and 31 is recycled via transfer intoand out of a suitable heat exchanger attached to both heating andcooling equipment, all having sufficient capacity so as to maintain thetemperature within the inner channels as desired. The inner channel ofspace 30, 73, and 72, provides space through which a continuous streamof fluid originating from annular space 80 can be transferred in thedirection shown by arrows 28, 38, and 32. Innermost discs 33, 52, and 4,are fixed rigidly to inner shaft 68, with bushings there between,represented by member 70 which comprises a series of bushings of similarlength located around inner shaft 68. Inner members such as 4, 52, and33, can be manufactured from any suitable material which may be organic,plastics materials of any suitable type, metals such as Iron with thesurfaces “nitrided”—a common term in the machine tool industry—and whichcomprises surface treatment to provide a thin layer of Iron nitride(Fe₂N); a special ceramic material comprising nickel and aluminumtreated in such a way that the two metals amalgamate to create a ceramicnickel aluminite (NiAl) or any other suitable material but mostpreferably will be inert or substantially inert. The equipment as shownin FIG. 2 can be integrated into a process capable of producing liquidfuels such as diesel and paraffin synthesized from a dense fluidcomprising carbon monoxide and hydrogen, known as “syn-gas”, in suitableproportions wherein said dense fluid originates from equipment asdescribed in FIG. 1. A suitable, gas tight connection between theequipment shown in FIG. 1 and FIG. 2 can be arranged such that thesyn-gas flows into the annular space 80 of FIG. 2 and maintained at asuitable pressure such as 10 bar or more or less, and having a suitablerate of mass flow. Syn-gas transferred into annular space 80 then flowsin the direction shown by, for example, arrows 28, and 32, which istransferred via reticulating channels radiating outward from the annularspace 80 and then returning toward the centrally located bushing shownas 70 and outwardly again in channels that radiate outward machined intoand across the surface of members such as 33 wherein said micro-channelsradiate outwardly along paths that intersect at the plan view centerpoint of members such as 33.*** shaft in direct contact with thesurfaces of 24, 82, 48, 50, 92, and 26, and in such a manner that willmaintain a substantially constant temperature such as between as low asminus 80 degrees C. and up to 450 degrees C. Catalysts, such as IronNitride (Fe₂N), Magnesium (MgO), Silicon Oxide (SiO₂), sintered Iron(Fe), Iron Carbide (Fe₂C) and Cobalt (Co) which have been crushed andbroken into pieces between 1 mm and 3 mm overall size can be packed intospaces represented by channel 30, 73, 72, 10, and 15, and such thatfluid transferred through the channels from an inner space 80 and in thedirection shown by for example arrows 28, 38, 1, and 40, will be indirect contact and exposed in such a manner that the specified anddesired reaction between the two gases hydrogen and carbon monoxide toproduce various other fluids such as ethylene, ethanol, diesel,paraffin, and polyolefins from which for example polyethylene andpolypropylene can be manufactured. Ethanol having the formula C₂H₆Oclearly requires oxygen to be present and this can be achieved byproviding super heated steam, carbon dioxide, or oxygen gas into annularspace 80 in proportions approximately equal to that required to produceethanol from a reaction between the gases of hydrogen and carbonmonoxide with said oxygen. In normal operation the equipment shown inassociation with FIG. 2 will produce a range of fluids which can beadjusted according to the prevailing temperature, pressure, and mostimportantly the type of catalyst provided in channels such as thechannel 72 and 73. It can be seen that the fluid in channels 72 and 73as indicated by arrows 32, 38, and 28, is moving as arranged in theopposite direction of the fluid medium transferred through space 15, 10,or for example 62, traveling in the direction for example shown byarrows 12, 1, and 40, so as to provide for a more consistent temperaturethroughout the equipment. It should be noted that members 33, 52, and 4,fixed to driving shaft 68, can be driven by rotating shaft 68 and indoing so provide a continuous mixing action for fluids transferred intoannular space 80 and along the channels such as 10 in the directionshown by arrows 32, and 28. Additionally channels can be machined intodiscs 33, and 52, for example and furthermore the proximity of discs 33,and 52, for example can be in close and touching proximity to theparallel walls shown as for example 24 and 34. The channels can bemachined so as to connect the annular space in contact with bushing 70radiating outward and to the perimeter of for example discs 33, and 52.Furthermore micro channels can be machined into the contacting face ofadjacent walls 24 for example and 34 providing an intensive mixingcondition to any fluids that are transferred through the channelsoriginating from annular space 80. In this way for example the equipmentdescribed in association with FIG. 2 can also be used for the productionof bio-diesel wherein the fluids comprising triglycerides, ethanol, andsuper critical carbon dioxide, can be transferred respectively throughthe inlet conduits 7, 8, and 6, and into annular space 80 at a pressuresuch as 2000 psi or more or less and there from via channel shown byspace 10, 13, 15, so as to provide for thorough blending of the threefluids as they are transferred through the equipment. It is anticipatedthat the reaction time for bio-diesel will be little more than oneminute, perhaps less, and unlikely though it is, somewhat more than aminute but certainly not more than five minutes.

Referring now to FIG. 2 (i) a cross section through equipment similar tothat described in association with FIG. 2, however the equipment shownis complete and provided with hydraulic pistons 900 and 920. Threestreams of 1) triglycerides, 2) SC—CO2 and 3) ethanol, are provided viathree high pressure conduits within heavy walled tube 921 and intoannular space 922 which is confined and subject to violent blendingaction by impellor 923. Annular space 922 communicates directly withconduit 924 which connects directly with annular pathway 926 which feedsthe first rotating disc space. Piston 920 and piston 900 are arranged toprovide hydraulically driven compressive force diametrically opposed toeach other to provide a clamping force P3. Piston 900 is pressurized inthe direction shown by arrow 927 while piston 920 is retained with acompressive clamping force in the direction of arrow 928 and such thatthe combined clamping force of piston 920 and piston 900 results in apressure of at least up to 3000 psi in the space between the twopistons. A series of drilled segmented conduits such as 902 are providedon a pitched circle diameter within the external edge of members such as914 and 929 and allow the flow of glycerol within space 902 at apressure similar to the pressure throughout the space between pistons920 and 900 which are retained within a common cylinder 904 whichcomprises a heavy walled steel tube with a honed surface finishthroughout and across the inner wall 930. Impellor members such as 931and 932 are rigidly attached to drive shaft 925 which is located at thecenter of cylinder 904 having centerline 933 common to both cylinder 904and drive shaft 925. Annular space 922 encloses a section of drive shaft925 connecting with conduit 924 which encloses a section of drive shaft925 also. A total of five impellers are provided clamped between memberssuch as 929 and 914 and arranged such that the blended proportionedfluid comprising a proportion from each of streams 936, 938, and 940,which represent triglyceride stream, super critical CO2 stream, andethanol stream respectively wherein the streams 936, 932, and 940, aretransferred into annular space 922 in adjustable and selectedproportions and at a pressure sufficient to provide for the continuoustransfer of the combined fluids into annular space 922 and there from toflow along disc space 926 between the first disc 942 which lubricatesthe space through which it is pumped in a radial and outward directionaway from centerline 933. The rotating discs such as 931 are driven byan electric drive 950 via a suitable gearbox thereby providing acontinuous and adjustable rotating shaft 925 which is connected directlyto the output of said gearbox. Each disc 931 is driven via a suitablekeyed connection thereto and the rotating speed can be as much as 3000rpm or more or less. The fluid comprising the processing liquidtransferred into space 922 flows radially outward and through a spacesuch as 952 and then between a second outer member such as member 929and in such a manner that the fluid prevents contact of the rotatingdiscs and the enclosing members such as 914 and 929. It can be seentherefore that fluid transferred into the equipment described inconnection with FIG. 2 (i) is firstly of selected proportions and thefluid is subjected to the pressurized fluid which flows around its upperand lower faces, thereby preventing contact with the members on eachside of said disc or rotor such as 961. A series of blades are fixedaround the perimeter of each disc and arranged to apply outward radialpressure to fluid which is in contact there with. Such outward radialpressure or centrifugal force results in the heaviest particles that maybe present with said fluid, in such a manner that the heavier matterwill occupy the furthermost available space within which it has directcommunication. Therefore any glycerol formed as a result of the reactionbetween the three components of fluid transferred into space 922 will bedriven into space such as 956 and progressively spaces such as 956,which are provided around each disc or rotor, will become filled withglycerol and the action of each rotor will cause any fluids of lowerdensity than the glycerol to occupy available space inward of theaccumulated glycerol, and the deeper said glycerol becomes in the spacearound each rotor such as 956, the more pure it will become at theregion furthest away from the peripheral impellor type blades such as958. Each pair of members enclosing respective rotors have an annularrim such as 912 which contacts the face of the opposing member such as914 which is in direct contact with annular ridge 912 which is arrangedto provide a seal when pressurized suitably. The pressure between a pairof members such as 914 and 929 can be adjusted by adjusting the glycerolpressure P2 relative to the pressure of fluid transferred via annularspace 922. More specifically when glycerol pressure is lowered relativeto the pressure at, for example 956, the members such as 929 and 914 canbe caused to open and the pressure difference between the two fluidswill only equalize after fluid has transferred from the inner spacessuch as 956 and into space such as 902. This is in fact the manner inwhich glycerol, having accumulated in spaces such as 956, can be removedfrom the stream of 952.

Referring now to FIG. 3 an equipment designed for the purpose ofgasifying carbon with super heated steam to produce carbon monoxide andhydrogen gas comprises a tube manufactured from inconel steel with anouter wall 2002 and inner space 2000. The process of syn-gas productionin this way is also described as steam reforming. The inconel steel tubeis enclosed within an outer shell 2004 and an 2014 can be filed with anysuitable metal including inconel and alternatively could be for examplezinc having a melting point below 400° C. The equipment is heated byeither electrical induction or electric heating elements provided withspace 2014 and at suitable locations therein to ensure a consistent andstable temperature throughout the length of said Inconel tube 2002within the outer shell 2004. A port 2016 represents the injection portthrough which super heated steam and carbon powder is transferred and asuch a velocity and mass flow that the residence time within space 2000of tube 2002 is not more than one second. FIG. 3 shows entry port 2016as an open end of inconel tube 2002 however a preferred embodiment maycomprise an extended tube section connected to port 2016 and whereinsaid tube extension is enclosed within a suitable heating means such aselectric band heaters attached to the full outer circumference of theinlet tube having sufficient heating capacity to generate super heatedsteam from water contained in the suspension injected therein by way ofa suitable high pressure pump continuously and at rate of injectionsufficient to ensure that the residence time for any particularparticulate suspended in the water injected therein. In this way watercontaining granulated or powered carbon wherein the particulate size ofsaid carbon does not exceed 30 microns and most preferably 10 microns.When assembled as described in association with FIG. 3 and the capacityto gasify carbon by reforming with super heated steam is substantial. Asuitable high pressure pump such as can be supplied by Bran & Luebbecomprising most preferably a positive displacement diaphragm pump isprovided an unlimited supply of powdered carbon blending in suspensionwith water provides the source materials and the pumping means to enabletransfer of sufficient carbon and water into space 2000 or inconelconduit 2002. When provided in this manner the subsequently vaporizedwater expands with explosive force driving the suspended carbonparticles through conduit 2002 and around each spiraling segment of saidtube 2002 and in manner that ensures contact with the walls of tube 2002by way of centrifugal force. The specific density of super heated steamis substantially less than the specific density of solid carbonparticles however given the adequate flow of super heated steam throughconduit 2002 in the direction shown by arrow 2006 and arrows 2016 and2018 ultimately arrow 2020 and 2022. The carbon particles are carried athigh velocity through conduit 2002 ensuring a contact with the innersurface of conduit 2002 thereby ensuring that gases transferred throughconduit 2002 occurs more rapidly than does the solid carbon particles.In this way continuous contact within the spiraling section of conduit2002 in conjunction with the high velocity with gases therein ensuresthe disturbance of carbon monoxide and hydrogen production by thereaction of said super heated steam with said carbon particles. Thismethod enables contact of the carbon particles intimately with superheated steam thereby ensuring that the reaction is maintained.

Referring again to FIG. 3, conduit 2002 is directly attached to aconduit extension terminating at an injector 2048 and mass flowregulator 2046. A fluid suspension comprising water, glycerol which canbe included optionally, and carbon “flour” is pumped under high pressurein the direction shown by arrow 2042 through conduit 2040 to mass flowregulator 2046 with computer controlled flow regulation having lowvoltage control connecting mass flow regulator 2046 with PLC connectionwhich provides the means to regulate the fluid input according torequirement via conduit 2050 via injector 2048. The entire length ofconduit 2050 and 2002, and vessel 2004 with the enclosed spiral conduitis heated by way of electric induction or alternatively any suitableheating method including the injection a quantity of oxygen directlyinto the flow wherein the quantity of oxygen is controlled with preciseaccuracy but enabling combustion of sufficient carbon with the conduitto generate heat to elevate he temperature to approximately 850 C. orhigher or lower. In this way water contained within the fluid injectedin conduit 2050 is rapidly converted to super-heated steam with theenclosed straight-section conduit at 2050 and 2002 in addition to thespiral 2003 and straight section 2051. The rapid expansion of volume in2050 and 200 causes massive velocity increase in the direction shown byarrow 2006. The straight input section of 2050 and 2002 enables anunrestricted increase in velocity of the super heated steam carryingwith it the carbon “flour”. Carbon “flour” comprising carbon particleshaving particles of 30 microns maximum diameter but typicallysubstantially smaller are carried with the super heated steam and driveninto the inner face of the outer wall of each spiral such as at 2030. Inthis way the carbon particles roll over the inner surface of thespiraling conduit and therefore travel at a substantially lower velocitythan the driving super heated steam which is present in overwhelmingquantities. The reaction between water and carbon to produce the gaseshydrogen and carbon monoxide is enhanced by disturbing the outward flowof the gases from each carbon particle thereby improving exposure ofeach carbon particle to the super heated steam and more importantlyoxygen and hydrogen atoms which drives the reaction. The resultingsyn-gas blend (CO, H₂ plus excess water vapor) expands and thereforeaccelerates in velocity, as it travels through the spiraling section2003 and subsequent straight section 2051 in the direction shown byarrow 2022, until all free carbon, carried with the gases, ash and superheated steam/water vapor, is consumed. The ratio of firstly, the entireconduit length to the quantity of carbon micro-particles suspended inthe stream of water injected therein is arranged so as to maximize theefficiency of syn-gas production; more particularly, the measured andcontrolled quantity of carbon particles suspended in water and injectedinto the input end of the inlet pipe is sufficient to facilitate thecontinued reaction of the superheated steam with carbon “flour” ormicro-particles until the remaining carbon is consumed as it is carriedthrough the straight section 2051 and until just prior to thecombination of syn-gas, ash solids and excess steam is dropped into thecyclone shown as item 48 in FIG. 1. The temperature is maintained at ahigh level such as in the order of 850° C. and the pressure can exceed5,000 psi but a minimum of 3,000 psi is preferably maintained. Atapering restriction at 2024 terminates in a profiled restriction at2039 wherein as shown in FIG. 3 (i) with radially arranged narrow slotlike apertures 2032, 2034 and 2036 radiating outward from a smallcentrally located round aperture 2038, provides the conditions toconvert any remaining carbon particles to syn-gas. Most preferably, theslot profiled openings such as 2036 will be no wider than 200 microns.The conduit expansion at section 2026 allows the syn-gas generatedwithin the conduit to expand into a wider section of the conduit at 2012and the continuous flow of syn-gas continues in the direction shown byarrows 2010 and 2008. Port 2028 connects directly with an ash separatingcyclone, shown in FIG. 1 as item 48.

The equipment shown in FIG. 3 may be integrated into a system similar tothe arrangement as shown in FIG. 1 by inserting it such that conduit 92of FIG. 1 is connected directly to port 2016 of FIG. 3 and port 2028 iscoupled directly to port 102 of conduit 100 also of the FIG. 1.

Referring again to in a preferred embodiment, exhaust gas containingcarbon dioxide can be collected by way of conduit 450 wherein arelatively high volume but low pressure compressor at 452 compresses thecollected gases to provide a stream of exhaust gases that travel in thedirection shown by arrow 454 prior to compression and after compressionat a relatively low pressure (for example, in the order of 50 psi to 80psi) the compressed exhaust gases are discharged into conduit 456 so asto flow in the direction shown by arrow 458 and after transfer throughmultiple filters 460 are released through a diffusing member 462 locatedat the base of pressure vessel 464, most preferably comprising acylindrical stainless steel enclosure with domed ends, having a diameterapproximately ⅙^(th) of it's length and enclosing space 466 within thepressure vessel 464. Pressure vessel 466 is filled up to about 60% ofits volume with fluid polyamine to a level indicated by line 468.Pressure relief valve 470 is arranged to be in direct communicationbetween space 476 and the external atmosphere and is located at theuppermost region of vessel 466 and above region 476 of space 466.Conduit 472 is located at an upper region of vessel 464 and in directcommunication between region 476 of space 466 and atmosphere such thatexcess gas that may otherwise accumulate in region 476 can dischargedirectly to atmosphere via conduit 472 and in the direction shown arrow474. Vessel 466 is rigidly mounted to a suitable carbon steel frame (notshown) with identical pressure vessel 478 located adjacent to andparallel and at the same level with vessel 478 which is also mountedwithin a carbon steel frame such that liquid polyamines can betransferred between the two pressure vessels 464 and 478. A purpose forusing polyamines in this way is to enable the selective absorption ofcarbon dioxide gas from a continuous stream of exhaust gases wherein thesaid exhaust gases comprise nitrogen and carbon dioxide substantiallywith trace gases including oxygen, carbon monoxide and atmospheric inertgases. Polyamine liquid selectively absorbs carbon dioxide gas at alower temperature of for example 45 F and can be expelled or removedthere from by elevating the temperature of the polyamine fluid.Therefore when fluid polyamine is transferred into vessel 478 and heatedby way of for example gas furnace 482 carbon dioxide gas having beenabsorbed into the polyamine fluid is released there from in gaseousphase and will accumulate within space 480 within vessel 478. Pump 484can be conveniently located at an upper level relative to and adjacentto vessels 478 and 464 and arranged with conduit communicating directlywith an upper region of vessel 466 and having discharge conduit 492communicating directly with a lower region of vessel 478 with anopposing pump 486 arranged to extract polyamine fluid from an upperregion of vessel 478 and arranged to extract polyamine fluid from vessel478 and discharge into a lower region of vessel 464. As can seen the twopressure vessels 478 and 464 containing polyamines filled to levelsindicated by lines 468 and 481 with interconnecting conduits 496 and 471and pumps 484 and 486 respectively can be arranged to convenientlyextract carbon dioxide gas from a continuous stream of exhaust gasestransferred via conduit 450 being drawn thereto by compressor 452 toselectively remove carbon dioxide gas from said exhaust stream andtransfer into an isolated enclosed space 480 and therefrom as shown byarrow 482 and 492 along conduit 494 directly to compressor 408.

Referring again to and in particular to gas diffuser 444 most preferablya diffuser having a capacity to process gas transferred there-throughproducing micro-bubbles having a diameter of less than 1 mm. In this waythe surface of carbon dioxide gas in contact liquid carbon dioxide isincreased substantially compared to bubbles having larger diameter andthereby enabling the rapid condensing of gas to liquid phase carbondioxide. The heat exchanger 440 can be arranged to reduce thetemperature of liquid carbon dioxide in the conduit 438 in the directionof arrow 446. Refrigeration 400 is powered by electricity mostpreferably generated by hydroelectric-produced power. In this way themethod of separating carbon dioxide from the exhaust stream of anyCO2-producing generator. By selectively dissolving into polyamine fluidwhile allowing the remaining atmospheric gases such as nitrogen thecarbon dioxide is retained and energy is not wasted in the compressionof inert gases and having no effect on atmospheric conditions. Theatmospheric gases are allowed to escape through conduit 472 in thedirection shown by arrow 474 and the carbon dioxide-laden polyamine istransferred from vessel 464 and into vessel 478 by extraction from anupper region within space 466 by pump 484 which them transfers thepolyamine medium to a lower level of vessel 478. By elevating thetemperature of the polyamine in vessel 478 the carbon dioxide gas isrelease into space 480 and as the pressure builds within space 480carbon dioxide gas is extracted in the direction shown by arrow 482through conduit 494 and eventually to compressor 408. The gas pressurewith space 480 can be allowed to elevate thereby reducing thedifferential pressure between the inlet pressure in the direction shownby arrow 412 such that a relatively small amount of energy is consumedin compressing the gas so as to overcome backpressure exerted by theliquid carbon dioxide in space 432 of vessel 424. However thetemperature of liquid carbon dioxide with vessel 424 will increaseprogressively and must therefore be dealt with hence the installation ofheat exchanger 440 connection with refrigeration 400. Excess liquidcarbon dioxide them be extracted via conduit 426 in the direction shownby arrow 426 and transferred to a suitable transfer facility by mostpreferably directly into road or rail shipping tankers by road or rail.In this way large quantities of carbon dioxide gas can be collected andconverted to dense liquid at minimum cost in terms of energy andequipment. It should be noted that the conversion of carbon dioxide gasat atmospheric pressure to liquid phase carbon dioxide at 0 F and 300psi which is the universal storage standard of pressure and temperatureat which typical shipping tankage can be used to maximum benefit. Afterthe removal and processing of the exhaust carbon dioxide from theatmosphere it can sequestered by transfer to a suitable space such asbelow ground in a non-productive oil well having been drained ofprofitable crude oil. The transfer of liquid carbon dioxide to storagespace below ground provides a safe storage arrangement that is likely toremain below ground for many thousands of years. Furthermore thetransfer in the way to substantially depleted oil wells can result incorresponding quantities of oil there-from.

The equipment described in association with, and the method used toseparate and collect carbon dioxide gas from any exhaust stream can alsobe used on a small scale such as gas turbine generation of electricityand also from automotive exhaust sources. Perhaps the most challengingproblem that must be overcome is the removal of carbon dioxide fromautomotive exhaust and particularly the rapidly expanding fleets ofsmall vehicles. In a preferred embodiment the principles disclosed inassociation with can be applied on a small scale in particular for usewith sport utility vehicles and prime mover tractor/trailer trucks thatcontinue to increase in number. The insertion of a hydraulic pumpbetween the power takeoff drive and differential drive input locatedbetween the engine and the rear axle can be arranged such that when thebrake is applied to any of these vehicles the hydraulic pump is engagedso as to pump at very high pressure for example 20,000 psi or more orless. Suitable hydraulic fluid pumped into a heavy spring-loadedaccumulator thereby storing energy as a compressed reservoir which canthen be applied to drive a relatively low pressure compressor whereinthe exhaust stream or a major part thereof can be redirected into asuitably sized accumulator of exhaust gas generated by the vehicle'smain engine. Following the capture of exhaust at elevated pressure astream of the stored exhaust is transferred through a atomizing manifoldand into a vessel substantially filled with polyamine. Nitrogen gas canthen be immediately released to atmosphere while the undesirablenitrogen compounds can be also collected in a separate container. TheCO2 gas is derived from the exhaust stream is then reduced to liquidphase carbon dioxide and stored in a high pressure vessel until theopportunity to remove it.

Referring now to an outline of equipment is shown in diagrammaticformat. Three pressure vessels 424, 478 and 464 are shown with variousconduits connecting therewith are provided to comprise an assembly withcompressors and pumps arranged so as to selectively separate andtransfer carbon dioxide gas represented by arrow 412 from a continuousstream of exhaust gases represented by arrow 454, after extractiontherefrom in the direction shown by arrows 414, 420, and 442, withexcess liquid carbon dioxide extracted in the direction shown by arrow426 from conduit 428. Suitable valves are provided as required tomaintain a pressure of approximately 300 psi to 350 psi in space 432. Anexpansion valve 430 is located at the upper end of pressure vessel 423and a valve controlling inlet pressure at 444 is also provided. A heatexchanger 440 is connected via conduits 438 and 402 to pressure vessel424 so as to allow the extraction of liquid CO₂ from an upper level ofpressure vessel 424 and in the direction shown by arrow 446 directly toheat exchanger 440 via suitable valves and pressure regulators such as448 and then after a reduction in temperature, returning via conduit 402in the direction shown by arrow 450. A refrigerated compressor 400 islocated adjacent to heat exchanger 440 and arranged to have sufficientcapacity to accommodate the heat load created by the equipment and thetransfer of gases therein. Gases comprising substantially carbon dioxideare transferred along conduit 410 in the direction shown by arrow 412 tocompressor 408. Compressor 408 may be a screw type compressor, a turbinecompressor, or a combination of screw and turbine compressors, buthaving sufficient capacity to compress CO₂ gases emitted by firstly, theABP meat processing equipment as described in patent applicationsdisclosed in the name of the present inventor, or secondly CO₂ generated(at a rate of approximately 500 tons per day) by ethanol production fromfermenting corn or thirdly, the vast quantities of carbon dioxide gasproduced in the numerous coal fired electricity generating plantslocated throughout the world including the USA, Australia, and China.The purpose of the equipment disclosed in association with is to providea relatively low cost equipment with the capacity to reduce the carbondioxide exhaust gases of such plant as coal fired electricity generatinginstallations. The ABP beef separating plants will be used as pilotplants in the development of the massive equipment required for eachcoal burning facility. The carbon dioxide used by the ABP beefseparation facilities in insignificant, and furthermore carbon dioxideproduced at the ethanol production plants and therefore is not adding tothe CO₂ load of the earth's atmosphere. It is clear that a low costequipment capable of removing CO₂ from the atmosphere by preventing theescape of encapsulated exhaust streams discharged from the massive coalburning plants now proliferating China in a world that is alreadyproducing too much carbon dioxide. The equipment shown in associationwith is simple and does not require the installation of massive CO₂compressors that are horrendously expensive even for small quantitycompression let alone the massive quantities produced by coal burning.Returning to gas exhausts produced by burning coal can be directedthrough a series of membrane filters that will separate nitrogen andcarbon dioxide substantially. The stream of CO₂ and nitrogen whichcomprises predominantly nitrogen, is separated such that the majority ofnitrogen is returned to atmosphere with a very small percentage ofcarbon dioxide and the substantially carbon dioxide stream containsapproximately 8% to 10% nitrogen with a balance (90% to 92%) of carbondioxide. Nitrogen is separated prior to transfer through conduit 410 inthe direction shown by arrow 412. The turbine compressor 408 increasesthe pressure to approximately 400 psi and transfers the stream throughconduit 416 in the direction shown by arrow 414 through filters 404 and406 installed in the stream of conduit 418 and the filtered fluid isthen transferred in the direction shown by arrow 420 via conduits in thedirection of 442 to inlet valve 444 which releases at a controlled ratea stream of fluid carbon dioxide into the liquid carbon dioxide whichsubstantially fills space 432 of pressure vessel 424. Pressure vessel424 may comprise a section of stainless steel tube of 6 inches diameterand of sufficient length that the gas transferred therein whichcomprises more than 90% carbon dioxide will enable the carbon dioxidecomponent of the gas stream to condense into liquid while the smallquantity of nitrogen that remains in bubbles will continue to travel inthe direction shown by arrow 434 into the space 448 which isperiodically exhausted via pressure regulator 430 to atmosphere. Theliquid CO₂ in space 432 is recycled via a heat exchanger 440 with anextraction port connected to conduit 438 at an upper location inpressure vessel 424 such that a controlled flow of liquid carbon dioxidecan be transferred in the direction shown by arrow 446 through vein pump448 into heat exchanger 440 which can be a tube in shell heat exchangermanufactured from carbon steel or stainless steel but wherein the shellis filled with a suitable refrigerant which may be ammonia or evencarbon dioxide and a tube is provided to allow for the transfer of theliquid CO₂ from pressure vessel 428 into the heat exchanger tubes andthen there from through conduit 402 in the direction shown by arrow 450.The arrangement is provided such that the temperature of liquid CO₂ inspace 432 will be maintained at between minus 10 and up to 20 degrees F.and at that temperature which will most efficiently provide for thecondensing of compressed gas transferred therein from the compressor408. Liquid CO₂ is returned to pressure vessel 424 via a port located ata lower section of the pressure vessel via conduit 402 in the directionshown by arrow 450. A refrigerated compressor 400 is connected to asecond heat exchanger in parallel with heat exchanger 440 and isarranged to allow air cooling of the refrigerant medium after transferthere through prior to its use to chill the liquid CO₂ of vessel 424 inthe heat exchanger 440. Atmospheric air can used but most preferably aheat exchanger is connected with refrigerant compressor 400 so as toallow the refrigerant to be chilled by heat exchange with a medium suchas glycerol which is reticulated through the other side of the heatexchanger, in fact any suitable liquid medium can be employed as arefrigerant on the heat producing side of the heat exchanger andglycerol or an equivalent blend of similar fluid that can “absorb” andcarry heat away from the heat exchanger to another location wheretransfer of the excess heat can take place. In a preferred embodiment,the heat provided by the condensing CO₂ vapor within vessel 424 can mostpreferably be applied to another useful process such as a drying aidwherein for example, solid fuel such as XXXXXX is produced and is blownvia suitable fans in the direction shown by arrows 436 so as to flowacross and in intimate contact with the heat exchanger provided tocontrol temperature of the refrigerant medium used in refrigerationcompressor 400.

Inconel® 600 or 625, INCOLOY® alloys 800H and 800HT® manufactured byPrecision Cast-parts Corp (PCC), Portland, Oreg., are examples ofsuitable materials from which the above higher temperature applicationequipment can be built.

Referring to FIG. 6 (i) and FIG. 6 front elevations of equipment thatcan be utilized for the gasification of a continuous stream of superheated steam and carbon particles is shown. FIG. 6 (i) shows a frontelevation of an “in situation” assembly of three pressure vessels 6116,6077 and 6075 and FIG. 6 shows a front elevation of a single pressurevessel identical to each of the three pressure vessels in FIG. 6 (i)however the assembly shown in FIG. 6 shows detail of each end (upper andlower) with a central section absent for clarity. A cross sectionthrough each of the three pressure vessels of FIG. 6 (i) and the singlepressure vessel of FIG. 6 would detail a circular cross section withheavy wall section however in FIG. 6 the central section of the sketchindicates a circular cross section by way of 3-D imaging of partsindicated and with the upper and lower aspects cross-sectioned to showthe contents wherein the cross section passes through the centerline ofthe representative pressure vessel.

In a preferred aspect of equipment detailed in FIG. 6 and FIG. 6 (i) theassembly includes an input port 6042 through which water and pulverizedcarbon particles can be transferred after heating as shown by the arrow6040. Multiple extraction conduits such as 6002 and 6056 can be arrangedaround the central input conduit 6044. The pressure vessel comprising aheavy wall tube 6030 manufactured from a suitable metallic material suchas Inconel® 625 is enclosed at each end with suitably dished profilesuch as 6035 and 6049. The pressure vessel encloses space 6008 and 6028such that only a single input conduit 6044 with port 6042 and a multipleextraction conduits 6002 and 6056. Said input conduit 6044 extends thefull length of each pressure vessel held in position at the uppersection by member 6050 which can be riveted or welded in position but inany event attached so as to provide a sealed input conduit with safetyfactor according to American Society of Mechanical Engineers (ASME)requirements. A dimpled jacket 6066 with dimples such as 6068 isprovided around the outer surface of the upper section of each pressurevessel so as to provide a heat exchanger 6010 with passages such as 6012between the inner wall 6007 of pressure vessel 6001 and outer wall 6011sealed to enclose spaces between the inner pressure vessel and the outerwall 6011 and situated in such a way any fluid transferred in thedirection shown by arrow 6044 through inlet port 6062 and extractionport 6005 enabling the extraction of fluid in the direction shown byarrow 6006. Any fluid transferred via port 6062 into space 6012 andsubsequently extracted therefrom via port 6005 will be subjected tointimate contact with the outer surface of pressure vessel 6007 and inthis way heat can be removed from the upper section of pressure vessel6007 and by controlling the mass flow of said fluid transferredtherethrough the internal temperature of space 6008 can be affected. Ifsaid fluid transferred via space 6012 is maintained by means of anexternal heat exchanger at a temperature below that of space 6008 thenthe temperature within pressure vessel 6007 can be reduced however ifsaid fluid transferred via space 6012 is maintained at a temperatureabove that of 6008 then the temperature within said chamber 6007 can beaffected to the extent of elevating the temperature within said pressurevessel. In this way a selected temperature can be maintained within theupper section of said pressure vessel 6007. FIG. 6 (i) shows theassembly of pressure vessels 6116, 6077 and 6075. The pressure vesselsare enclosed within insulating jackets 6090, 6073 and 6071 respectivelyeach enclosing the upper portions of each pressure vessel above theenclosure 6015 and the segment of each pressure vessel enclosed withinenclosing walls 6084 below the horizontal upper perimeter of enclosingwalls 6015 with electric induction or otherwise heating arrangement 6086arranged so as to heat the lower sections of each pressure vessel. Inthis way the entire pressure vessel can be maintained at a selectedtemperature such as any temperature such as between 600 C. and 1,100 Ctherefore. Water is first transferred via inlet port 6062 and outletport 6005 prior to superheating and then in a continuous stream blendedwith a controlled continuous flow of carbon particles and mixedtherewith prior to transfer via conduit 6044 as shown by arrows 6040 and6052 along the full length and in a downward direction within each ofthe pressure vessels 6116, 6077 and 6075. Each pressure vessel isarranged similarly with members 6049 and 6037 providing passagewaysallowing transfer of superheated steam and carbon particles blendedtherewith in the direct shown by arrows 6085 and 6083 so as to emergevia a continuous annular slot at 6034 and 6082. A collection of hardchromed steel ball bearing such as 6078, 6079, 6081, 6033, 6076, 6016and 6070 are provided within space such as 6028. A fluid metal such as ablend of molten aluminum, nickel, and/or silver is provided andmaintained at a temperature above 600 C and most preferably at atemperature not more than 1,300 C. It must be noted that the materialfrom which pressure vessel 6016 must be a suitable metal able towithstand temperature and pressure to which it is subjected withoutendangering the operation of the equipment described herein. Superheatedsteam and carbon particles transferred via conduit 6044 along theenclosed space thereof and in the direction shown by arrows 6052 and6073 and then into space enclosing arrows 6083 and 6085 can bepressurized by a suitable high pressure pump such that the fluid blendemerges within the pressurized and enclosed space such as 6029 andtherefore forced most preferably in micro-bubble condition through theannular space represented by 6082 and 6034 and with such an expandingenergy caused by the exploding condition of superheated steam upward inthe direction shown by 6023 and 6080 so as to drive ball bearings 6033and 6081 upwardly shown by arrows 6023 and 6080 through the fluid moltenmetal and in the direction shown by 6020 and 6074 until the expandingenergy released with the explosive force delivered by superheated steamis spent and thereby resulting in ball bearings returning to the lowersection of pressure vessel in the direction shown by arrows 6070 and6018. Ball bearings returning to the lower region of each pressurevessel will provide disturbance of the fluid within space 6028 which canbe maintained at such a temperature that it vaporizes while withinregion 6028 and condenses within region 6008 and in the way providing aoverwhelming heat concentrated within the confining space of thepressure vessel. In this way the conditions within the enclosed space ofeach pressure vessel will result in the rapid gasification of carbonreacting with steam provided therein.

In this way substantial volumes of superheated steam and carbonparticles transferred via conduit 6044 can be converted by gasificationinto carbon monoxide and hydrogen gas rapidly. It is proposed thatassemblies comprising multiple pressure vessels manufactured fromsuitable materials such as INCOLOY® and INCONEL® metals manufactured byPCC can be arranged most preferably within buildings no longer used inthe aluminum smelting industry which are available in the PacificNorthwest of the United States of America with the abundant availabilityof hydroelectric power available from the hydroelectric power plantsadjacent to the former aluminum smelting plants.

Referring to FIG. 6 (ii) a cross section through a Fischer Tropschequipment is shown. This equipment is arranged so as to be scalable andin the example shown in FIG. 6 (ii) the cross section is suitable forrelatively small quantity production. Hitherto a typical gasificationand Fischer Tropsch renewable fuel production facility would be arrangedwith a capacity in the order of 200,000 barrels processing capacity perday. This represents some 8.4 million gallons fuel such as syntheticdiesel per day whereas the equipment contemplated in association withFIGS. 6, 6 (i), and 6 (ii), the production capacity of 1,000 barrels perday represents some 42,000 gallons per day. The equipment disclosed inassociation with FIGS. 6, 6 (i), and 6 (ii), can be arranged accordingto the outline of system components detailed in association with FIG. 7wherein one or multiple system components can be installed to operate inparallel thereby providing for any production output capacity from 1,000barrels per day or below, and upward to even as much as 50,000 barrelsper day. A major benefit available with the arrangement of equipment asdisclosed within this entire disclosure is the ability to producemultiple Fischer Tropsch fluids from a common syn-gas source which inturn having been produced by gasification of carbon derived from thereduction of multiple raw material sources such as biomass in the formof mulched green timber, mulched wheat straw, hay, or sawdust, from anysources even from timber pallets for example no longer useful due tobreakage; timber from any building site no longer required, this caninclude discarded fencing materials, garden clippings, trees removedfrom any site such as close to housing endangered by the tree. Thegasification equipment as shown in FIG. 6 will most preferably bearranged wherein the pressure vessel 6030 with heat exchanger 6010 ismanufactured from the preferred material INCONEL, is utilized in themanner disclosed with inlet conduit 6044 transferring a fluid suspensioncomprising water and carbon particles with other dissolved gases andfluids derived from the biomass carbonizing process into the manifoldarrangement comprising members 6049 and 6037 with metal balls (i.e. ballbearings) 6079, 6033, 6078, etcetera, and most preferably fluid metal6028 chosen from a short list of metals such as nickel and the alloysfrom which it can be manufactured. The liquefying of said metal nickelmay also include other metals such as zinc, and/or tin with silver andaluminum and any other metal listed below with the corresponding meltingpoint and boiling point listed therewith. The intermittent explosiveeffects of the water component of the carbon particle suspensiontransferred in the direction shown by the arrows 6083 and 6085 willproject the metal balls upward and away from the lower region of eachpressure vessel such as 6116, 6077, and 6075, shown in FIG. 6 (i). Thetemperature and pressure within the enclosed space of each pressurevessel can be maintained so as to not exceed the boiling point of themolten metals by a margin of +50 degrees C. or less and the resultantenvironment within the elongated free space surrounding the inletconduit such as 6044 shown in FIG. 6 and within the outer pressurevessel such as 6030 can enhance the reaction between water and carbonsignificantly so as to not only ensure the complete reaction of allcarbon occurs completely with excessive super heated steam transferredfrom within the enclosed space of each pressure vessel through the arrayof extraction conduits such as 6002, and 6056, in FIG. 6 in thedirection shown by arrows 6000, and 6054, respectively or in thedirection shown by arrows 6092, and 6108, of FIG. 6 (i).

METAL MELTING POINT BOILING POINT Platinum 1768.3° C.   3222° C. Cobalt1495° C. 2870° C. Nickel 1455° C. 2913° C. Copper 1084° C. 1984° C. Gold1064° C. 2807° C. Silver 961.8° C.  1762.0° C.   Aluminum 660.4° C. 1220.7° C.   Zinc 419.6° C.  787.2° C.  Tin 231.9° C.  449.4° C. 

The heat exchanger 6010 of FIG. 6 and heat exchangers 6112, 6114, and6110, of FIG. 6 (i), being located in the upper region of each pressurevessel and heat exchanger assembly provides a lower temperature by thetransfer of heat there from by way of a suitable fluid provided at asuitable pressure in an enclosed circuit wherein the fluid transferredinto port 6062 in the direction shown by arrow 6064, and subsequentlyafter reticulation through channels such as 6012 of heat exchanger 6010through extraction conduit 6005 in the direction shown by arrow 6006.All fluids so extracted are then transferred through a second (notshown) suitable heat exchanger arranged to reduce the temperature of theenclosed fluid ensuring that the temperature within each pressure vesselin the upper section of each pressure vessel is lower than thetemperature for example in space 6028 wherein a molten metal allows thesuper heated steam bubbles with carbon particles contained therein totransfer in the direction shown by arrow 6023 and 6080. In this way thevaporized metal or metals carried upward by the upward stream of syn-gasin the direction shown by arrows 6020 and 6074 will condense withinspace such 6008 allowing the syn-gases to be extracted in the directionshown by arrows 6004 and 6060 through conduits 6002 and 6056 while thecondensed metal with ball bearing such as 6070 will drop downwardly inthe direction shown by arrow 6018 and into the liquefied metal pool inspace 6028. It should be noted that molten metals such as fluid of space6028 can be extracted via a conduit connecting directly with the liquidmetals within space 6028 and in a manner that will carry with the fluidmetal extracted there from the ash solids that remain after reactionbetween carbon particles and super heated steam. Extracting liquidmetals in this manner which shall most preferably be collected at asuitable location above the liquid metal accumulating in the lowerregion of the pressure vessel and will most preferably collect thefreshly condensed metal as it flows down the inner surface of the outerwall 6072 of pressure vessel 6030. Liquid metal carrying ash in this waywith minimum quantities of carbon can be separated by way of a suitablecentrifuge prior to returning the molten metal into the inner region ofeach pressure vessel.

Any suitable liquid, element, or compound, can be used however mostpreferably tin or zinc, or a mixture thereof, followed by nickel orsilver are preferred. Any salt can be used that has a melting pointwithin the temperature range required which shall be maintained byelectrical elements installed around the vessel such as 6088 and 6036shown in FIGS. 6 and 6086 enclosed within walls 6084 of FIG. 6 (i). Theapproximate dimensions of vessel such as 6116 shall be approximately 10feet to 20 feet in length or height wherein the member 6037 is locatedat the bottom of the inside space and the member 6050 is mounted at theuppermost “crown” of the dome at 6001 and the internal diameter of theround cross section of the vessel 6072 shall be about 12 inches or moreor less. The conduit 6044 is profiled so as to be locked in place havinga length almost the full internal length of the enclosed space and thediameter of approximately 2 inches or more or less, comprising a heavywall round tube constructed of suitable INCONEL® high temperatureresistant steel mating with a centrally disposed extension of member6034 which is held in position between the inlet conduit 6044 and thelowermost member 6037 and arranged with space to allow free flowing offluid in the direction by arrows 6083 and 6085. Most preferably thepressure vessel will be provided with an entry port and most preferablymanufactured in two parts, an upper and a lower section connected at aflange portion of each member, bolted together with clamping means and agasket between the upper and lower sections. Insulation around the outersurface that would otherwise be exposed comprising a 6 inch thickinsulating layer 6090, 6073, and 6071 of pressure vessel 6116, 6077, and6110 respectively. A suitable storage pressure vessel can be provided toallow all syn-gas produced within each pressure vessel to be stored in acommon or series of pressure vessels.

Referring now to FIG. 6 (ii) an equipment arranged to synthesizeethylene (C₂H₄), ethanol (C₂H₆O), any diesel (having a formula of C₁₀H₂₂and up to C₁₅H₃₂) composition or paraffin (C₂₅H₅₂) is shown. Othermaterials such as naphtha (C₈H₁₈) from which olefin plastics (includingpolypropylene and polyethylene), can be manufactured by processingsyn-gas comprising a suitably proportioned blend of hydrogen and carbonmonoxide. The proportion of hydrogen: carbon monoxide (H₂:CO) can beadjusted by several methods including the injection of hydrogen gashaving been derived by electrolysis of water wherein hydrogen would becollected from one electrode and oxygen released to atmosphere from theother electrode. In the event that a larger proportion of carbonmonoxide is required, the hydrogen gas can be readily separated by wayof membrane filtering, but in each case a suitable catalyst is requiredto ensure the desired synthesis of the particular organic compoundoccurs. Such a catalyst may be any of the following: aluminum oxide(AL₂O₃); iron oxide (FE₂O₃); magnesium oxide (MGO); chromic oxide(CR₂O₃); silicon carbide (SIC); iron nitride (FE₂N); silicon oxide(SIO₂); sintered iron (FE); potassium oxide (KO); and cobalt oxide(CoO). Most preferably however, for the production of predominantlydiesel, a combination of iron, copper, magnesium, and potassium oxides,and silica gel broken into pieces of 1 to 3 mm in size, with 1% bismuthoxide, and then sintered by heating to a temperature at which thecatalyst is close to melting point and then pressed together in a moldwhich can be profiled as required, and when manufactured for use withthe equipment shown in FIG. 6 (ii) profiled in a disc shape having acentrally located aperture approximately one third the diameter.Sintered iron favors the production of ammonia whereas iron nitridefavors naphtha production, and magnesium oxide and silica oxide favorsparaffin production. Cobalt oxide should be included with all catalysts.It has been demonstrated that sintering by hot press and spark plasma,the most ideal particle size is in the order of 100 microns and thecatalyst blend should be heated in the presence of pure argon or gasatomized with pure argon.

The equipment shown in FIG. 6 (ii) comprises a drum shaped pressurevessel 836 with a centrally located hollow shaft 829 mounted withinsealed bearings or bushings wherein the hollow shaft 829 is press fittedwith a solid shaft 830 and welded together. The assembled shaft 829 and830 then allow fluids to be transferred via a central cavity 852 withinshaft 829 with passageways isolated so as to allow the transfer of arecycled temperature controlling fluid to heat exchangers arranged inalternate layers with sintered catalysts suitably profiled to provide astack arranged with shaft 829 centrally disposed therein. Moreparticularly a parallel sided drum shaped vessel 836 with round crosssectional profile, enclosed ends and extraction ports for surplus gasand synthesized fluids, and an internal diameter greater than theoverall diameter of centrally disposed heat exchanger and catalystsegments, allowing the rotation of the central shaft via a drive in thedirection shown by arrow 828, fixed to solid shaft 830, which in turntransfers a rotating force rigidly to hollow shaft 829 mounted in sealedbearings at 807 and 831.

Pressure vessel 836 comprising a parallel sided circular profile drumwith flat ends, having centrally disposed bearing mounts 831 and 807,shaft 829, with solid stub shaft 830 connected to suitable driving means(not shown), is mounted as a single stand alone equipment or multipledrums can be located in a rigid frame so as to provide an operatingstructure wherein each drum is operated in parallel with adjacent drums.Syn-gas, having been suitably trimmed, blended, and/or adjusted toprovide a stream of gas having a selected ratio of proportioned carbonmonoxide and hydrogen gas is transferred into conduit 802 in thedirection shown by arrow 800 at a suitable pressure of approximately oneor two atmospheres or greater and temperature in the range of about 180°C. to 240° C.; the reactions occurring in the production of theFischer-Tropsch liquids are generally exothermic. Said syn-gas passesvia conduit 843 and into and through each permeable catalyst annularring (alternately layered and “sandwiched” between a pair of temperaturecontrolling heat exchangers) such as 814, 816, 820, and 834. Arrows 811and 845 show the branching pathway of catalyst at location 814 and 816respectively, and other arrows show the entry point of said syn-gas intothe space filled by permeable catalyst. Suitably temperature controlledfluid such as glycol blended with water and optional selectedstabilizers, is transferred into conduit 848 at a suitable pressure inthe direction shown by arrow 846, through universal connection 804, andalong passageway 851 and 805 in the direction shown by arrows 850 and810. Each heat exchanger is profiled into a flat, parallel upper andlower sided, annular ring similar to each catalyst layer and in this waythe temperature of the catalyst layers is controlled by temperaturecontrolled (by way of an external heat exchanger) fluid mediumtransferred through each heat exchanger by way of a suitable positivedisplacement pump and transferred through each heat exchanger such as atthe layers indicated by the numbers 844, 842, 840, 818, 837; in this waythe fluid flows outwardly along the upper side of, for example, disc 813and simultaneously through similar passageways in all other heatexchangers such as 838 and 818, and then inwardly along the underside ofeach disc shown by arrow 825, after reversing direction of flowindicated by arrow 823, subsequent to passing along the upper side ofthe adjacent disc to arrow 821. Temperature controlling fluid is thenextracted via a universal connection 827 through conduit 826 and to anexternal temperature controlling heat exchanger in the direction shownby arrow 833. Syn-gas transferred via the most preferably sintered discmembers sandwiched under a selected pressure between each alternate heatexchanger layer by “0” rings such as 817 and 815 so as to ensure thesyn-gas passes through catalyst, reacting exothermically as the gasesreact while being transferred through the porous passageways of eachsintered, disc profiled catalyst. The centrifugal force generated by therotating shaft with all assembled discs therewith, encourages the rapidtransfer of liquids such as diesel away from the disc catalysts and intothe free space immediately inside the inner surface of outer vessel 836.Said fluid diesel, or other such fluid formed by exothermic reaction ofthe syn-gas within the sintered catalysts clamped between alternatepairs of heat exchanger discs, flows via the free space in a downwarddirection toward arrows 832 and 824 indicating the direction of flow ofthe resultant liquids produced by the exothermic reactions and throughconduit 830 and 858, and in the direction shown by arrows 860 and 862.In this way, selected diesel renewable fuels can be manufactured inquantities according to the availability of biomass derived carbon.Excess syn-gas will preferentially transfer in the direction shown byarrows 808 and 806 via conduit 864 which can then be recycled viaconduit 802.

Referring to FIG. 7 a block diagram illustrates the operating sequenceof the BTL (Bio-mass to Liquid) equipment disclosed herein where themodified extrusion system 5000 with input hopper 5002 shown in a planview of a typical equipment layout in block diagram format. Arrow 5004indicates the direction of flow of biomass and arrow 5006 represents thetransfer conduit from extruder 5000 to a suitable enclosed and sealedball mill, hammer mill or other suitable pulverizing equipment whereinthe stream of carbon transferred via conduit 5006 is pulverized toprovide a powdered carbon “flour”. Any remaining volatiles, gases and/orvapors generated during the biomass extruding process in extruder 5000are transferred into vessel 5018 via conduit 5022 and subsequentlycompressed prior to recycling through the system. A suitable enclosedblender 5018 is provided to allow suitable mixing of water and/orglycerol transferred therein via conduit 5016 via high pressure pump5024. The prevailing pressure within pressure vessel 5018 must bemaintained at or above the pressure within steam reformer 5012. Pressurevessel 5018 is disclosed in detail herein above in association with FIG.1 Items 58 and 26 and further comprises a temperature-controlledcondenser and/or diffuser through which gases can be transferred priorto blending with other fluids such as glycerol and/or water provided inquantities sufficient to dissolve any of the fluids transferred thereinvia conduit 5022. Temperature-controlling system 5026 is connected viaconduits represented by arrows 5028 and 5030 wherein a suitable mediumsuch as chilled water and/or glycerol or any other suitable refrigerantis transferred to vessel 5018 by a conduit represented by arrow 5028after being suitably chilled to a temperature of approximately 32 F. to40 F. The resulting fluid is transferred via conduit 5032 into highpressure pump 5034 and thence at elevated pressure such as 3,000 psi ormore or less via conduits 5020 represented by arrow 5020 to blender 5036wherein carbon “flour” and said fluid are blended together prior toinjection to steam reformer 5012. In another preferred embodiment saidcarbon “flour” may be transferred into vessel 5018 blended together withfluids therein prior to transfer to the steam reformer via conduit 5020after transfer through high pressure pump 5034. Steam reformer 5012 isdisclosed in detail herein in association with FIG. 3. However it shouldbe noted that two or any number of pressure reformers as disclosed inassociation with FIG. 3, can be combined together to provide a singlesteam reformer wherein syn-gas is produced comprising hydrogen gas andcarbon monoxide in a single stream.

Cyclone 5038 is coupled directly to steam reformer 5012 via conduit 5040and ash is extracted via conduit 5042 and suitable flow regulator whichmay comprise a compression screw within a suitably sized extruder asshown in FIG. 1 as item 152. Ash produced by the reaction within steamreformer 5012 any be combined with suitable fertilizer and used inagriculture according to agricultural procedures. Equipment includingextruder 5000 and steam reformer 5012 require a suitable heat sourcewhich most preferably will be hydroelectric tidal, wave or wind turbinegenerated. Extruder 5000 comprises a suitably profiled Archimedes screwwithin a matching barrel about which most preferably suitable bandheaters are installed. The temperature required to operate said extruder5000 is in the order of 500F however the temperature required for steamreformer 5012 may be as high as 950 C but most preferably between 600 Cand 850 C. Alternatively a percentage of carbon “flour” may be combustedwithin steam reformer 5012 by injecting oxygen gas continuously and inproportion to the stream of super heated steam and carbon “flour”causing combustion of up to 30% to 50% of the carbon “flour”. This willproduce carbon dioxide gas in large quantities which can be transferredwith Syn-gas to pressure vessel 5046 and collected in polyamine fluid asdisclosed above in association with. The carbon dioxide gas is separatedthereby from the stream and the remaining gases will comprisesubstantially all hydrogen and carbon monoxide which are transferred viaconduit 5046 to centrifugal reactor 5048 wherein the syn-gas isconverted to diesel and/or naphtha and/or methane or Ammonia or moreparticularly, as may be required according to the system operator andaccording to the catalysts provided therein such as Colbalt catalyst(Cobalt Oxide i.e. CO₃O₄) used in the production of Ammonia. Othercatalysts may be Tin oxide, Palladium oxide, Platinum oxide, or Titaniumoxide. Synthesized diesel fuel can then be pumped via conduit 5050 intostorage vessel 5052. Naphtha may be transferred topolypropylene-producing equipment 5054 via conduit 5060 and thentransferred via conduit 5056 to storage vessel 5058. If a polyolefinpolymer such as polyethylene is to be manufactured, which could beproduced by equipment located at 5054, the polyethylene polymer can betransferred via conduit 5062 to storage vessel 5064 and, after retentionin storage for a while, distributed to customers directly there-from.

Referring now to FIG. 8 and FIG. 9, a cross section through a pressurevessel 920 manufactured from heavy wall INCONEL 625 insulated with avacuum at 930 retained by outer vessel 934 with further heavy layer ofany suitable insulation 932 such as glass wall. Both ends of pressurevessel 920 are dish shaped and an extraction conduit 900 is locatedcentrally at the upper end of vessel 920 with insulation 904 enclosingconduit 900. A heavy heating element 926 manufactured from INCONEL 600is connected to anode 922 and cathode 924. Enclosed in space 918 is asubstantial volume of molten aluminum maintained at between about 900and 1300 degrees C. A floating separator 916 separates area 918 fromarea 908. Said separation wall 916 is provided with a skirt 934 and theentire skirt and separation member floats on the upper level of moltenaluminum 918. Separation member 916 is fitted with a metallic lip seal936 and can be manufactured from any suitable material but mostpreferably will be manufactured from nickel aluminum. Member 916separates molten aluminum contained in space 918 from space 908. Space928 represents about 25% of the volume of vessel 920 and a conduit 912with opening 935 is provided such that opening 935 is adjacent to thecenter region of separator 916. Space 908 is filled with super heatedsteam such that after transfer in the direction shown by barrow 912,distilled water including recycled water, is transferred via conduit 910and directly onto the surface of nickel aluminite separator 916. Saiddistilled water transferred through conduit 910 is most preferablyheated prior to transfer into chamber 908 via nozzle 935. Theorientation of the equipment shown in FIG. 8 with base 929 enclosedwithin any suitable enclosure and one that will ensure the uprightdisposition of the entire assembly such that heating element 926 can beactively heating the contents of space 918, i.e. molten aluminum. Itshould be noted that the electrical power required to operate theequipment shown here in connection with FIGS. 8 and 9 can be sourcedduring the off-peak hours of any day and the heat required to operatethe process wherein the temperature of molten aluminum 915. Four arrowssuch as 933 and 931 indicate the direction of convection currents withinthe space 918 which is transferred upward by convection currents and viathe nickel aluminite member 916 by transfer there through. The innersurface of member 915 at 940 can be lined with nickel aluminite andfloating member 916 and 934 is located adjacent to the exit port 935 ofconduit 910 such that when distilled water, which may also be recycledwater, is pumped through conduit 910 at a substantially constant rate,distilled water is projected directly at the upper surface of member916. FIG. 8 (i) is a cross section through the wall of vessel 920, 907,and 942, represented by insulation 967, vacuum 968, and outer wall ofvessel 964, and inner vessel wall 960 with nickel sheeting 963 locatedin position and against aluminum 967, both held firmly against innersurface of inner vessel 960 with vacuum space 968 and outer vessel 964enclosing vacuum of space 968. Insulation 967 is enclosed by outer mostvessel cover 990. The total thickness of nickel sheet 963 and aluminumsheet 960 is approximately 0.1 inches. Inner vessel 968 is manufacturedfrom INCONEL 600 or 625 while outer vessel 964 can be manufactured fromcarbon steel of approximately 2 inches in thickness or any otherstainless grade if required. Insulation layer 967 is in close contactwith outer vessel 964 and can be provided having any thickness 966 andmay be 12 inches to 18 inches in thickness. Outer cover 990 provided inpanels is fixed around the outer surface of insulation 967 so as toprevent damage to the insulation layer. Referring again to FIG. 8conduit 910 with opening 935 directs distilled water there through inthe direction of arrow 912 and directly at the upper face of separationmember 916. This member allows heat derived from the molten aluminum inspace 815 and upon contact of distilled water there with, vaporizationoccurs immediately and super heated steam generated thereby expandsoutwardly and upward in the direction shown by arrows 914 and 937. Thesuper heated steam may circulate within the space 908 until it escapesvia conduit 900 in the direction shown by arrow 902. This super heatedsteam can be transferred directly to conduit 9006 of FIG. 9 in thedirection of arrow 9004 or alternatively to input conduit 1200 in thedirection shown by arrow 1202 of FIG. 9 (i). Arrows 937 and 914, and909, 944, 942, and 907, indicate the swirling nature of super heatedsteam within chamber 908. The purpose of the equipment illustrated inFIG. 8 is to provide a means of storing heat at a very high temperaturesuch as between 900 degrees C. and 1250 degrees C. Aluminum melts below900 degrees C. and can therefore be retained in a molten conditionwithin space 918 for an extended period. Member 916 with skirt 934 canbe manufactured from nickel aluminite and is arranged such that it willfloat on the surface of molten aluminum within vessel 920. Electricitymost preferably will be generated by hydroelectric turbine, wind poweredgenerators or nuclear power plants methods and when used to heatelements 926 within space 921; the stored heat within the hightemperature molten aluminum therein can be used within a range of notless than 900 degrees C. and up to 1250 degrees C. It is important thatthe aluminum medium is retained in a molten fluid phase but belowboiling point or vaporization. The quantity of heat consumed willtherefore not exceed the total quantity of BThU's retained by saidmolten aluminum 915. Most preferably disused aluminum smelting plantslocated within the PNW and in particular, for example at the Dalles,Oreg., Longview or Goldendale, Wash. The existing electrical supply tothe aluminum smelting sites can be, most preferably, utilized to supplythe electrical power needed to heat the molten aluminum as required withthe equipment described in association with FIG. 8, to an upper limitbut below boiling point of the aluminum. The prevailing pressure withinspace 908 shall not exceed a safe level. Sufficient heat would beavailable by heating a aluminum smelting pots Heat Referring now to FIG.9 super heated steam transferred from conduit 900 of FIG. 8, in thedirection shown by arrow 902 is transferred via suitable insulatingconduit under pressure to input conduits 9034, 9016, and into conduit9006 after blending with a suitably proportioned quantity of carbonpowder/flour. A forged or other suitably profiled INCONEL tube 9038,closed at one end and open at a flanged upper open end, is connected toa flanged end of extension 9010 and attached together at flanges 9022rigidly and conduit 9044 is substantially filled with quartz sand so asto fill the lower ⅓^(rd) of the full length of the two conduit sections9044 and 9038. Super heated steam heated to over 1,000° C., or more orless, is transferred into jacket 9030 via conduit 9034 in the directionof arrow 9032 to facilitate the heating of and then maintain thetemperature of enclosed space 9012 and the contents thereof at the sametemperature (over 1,000° C., or more or less), while suitably pulverizedcarbon and superheated steam is transferred along conduit 9010 in thedirection of arrow 9004. Simultaneously, superheated steam at over1,000° C., or more or less, is transferred into space 9014 via conduit9016 in the direction shown by arrow 9018 in order to maintain thetemperature of conduit 9044 and its contents at over 1,000° C., or moreor less. More particularly, members 9033 and 9014 are attached directlyto each other by way of a clamp at 9022 and jackets 9038 and 9046 areprovided around the outer surface and perimeter of inner conduits 9010and 9045. Super heated steam is provided in 3 input streams to ensurethe temperature of enclosed space 9012 and of vessel 9038 and with inletport 9034 and exit port 9040. Steam travels in the direction shown byarrows 9032 and 9042. Quartz sand is used to provide a diffusing andmixing effect or mechanism at 9024, 9026, and 9028.

In this way carbon flour ground and pulverized to a “flour” consistency,and with the largest particles under about 30 microns across, and as mayotherwise be disclosed herein disclosed above, can be provided at lowcost for conversion to syn-gas for subsequent conversion to syntheticdiesel and olefins as may be required. Syn-gas is transferred in thedirection shown by arrow 9005 through conduit 9008 and transferred therefrom to the next operation which will likely be transferred into aFischer Tropsch. A further purpose of the present equipment is toprovide a suitable heat storage at above normal temperature. Referringnow to FIG. 9 (i) a configuration showing a steam reforming equipment isshown. An inner “L” shaped conduit 3012 is provided with a directcommunication to a source of carbon 3014 and a gas injection nozzle3020. A vertical section of said conduit 30010 is provided and in thedirection of arrow 3015 allowing the vertical transport of carbonmaterial along section 3001. Vertical section 30010 is enclosed by heatexchanging member 30011 with an inlet conduit 3006 allowing theinjection thereof via 3008 and extraction in the direction shown byarrow 30006 along conduit 30004. An outer vessel 3004 encloses the uppersection of said first transfer and micro style conduit 30010. Superheated steam transferred in the direction of arrow 3008 via conduit 3006of heat exchanger 30014 arranged in an inverted condition over theupward transfer tube 30010 and outer vessel 3014 encloses heat exchanger30014 so as to control the equipment. Hopper 30015 containing carbon3014 provides a continuous stream of carbon flour in the direction shownby arrow 3016 and transfer via screw member installed within conduit3013. In this way carbon flour is released into the upper side ofconduit 30060. Simultaneously super heated steam transferred in thedirection shown by arrow 3018 via conduit 3020 and in to space 3060thereby causing the mixing of super heated steam traveling in thedirection of arrow 3055 with carbon flour transferred from hopper 3015.Blended super heated steam and carbon flour is transferred underpressure via conduit 3012 and upward through conduit section 30010 inthe direction shown by arrow 3015 and is carried via space 3013 in thedirection shown by arrow 3019 and then in the direction shown by arrow3022 within outer vessel 3004 and into space 3014 by which time thereaction between super heated steam and carbon has caused the productionof carbon monoxide gas and hydrogen gas. Mass flow control 3028 controlssyn-gas transferring via conduit 3002 in the direction shown by arrow3000 and directly into Fischer-Tropsch fluids synthesizing reactor.

In another preferred embodiment, Fischer-Tropsch fluids, such assynthetic diesel (i.e. CnH₂n+₂, where n=any number from 1 through,typically, to a number less than 100), can be synthesized from a syngascomprising a first gas, (1) carbon monoxide component most preferablyderived from the endothermic reduction of carbon dioxide exhaust gas(from any suitable exhaust gas stream (4) source) toyield relativelyhigh purity carbon monoxide, with the second syngas gas, (2) hydrogencomponent being derived by collection from the isolated cathode ofselected electrolytic cell in a process comprising, most preferablyalthough not essentially, the acid (H₂SO₄) electrolyte enhancedelectrolysis of water.

The carbon monoxide and hydrogen gas can be produced with the followingprocess:

I Production of Carbon Monoxide Gas (1);

Carbon derived from any suitable bio-mass source such as coal (includingat least an adequate quantity of sulfur containing coal) is used as afuel to generate electricity in a typical coal fired power plant. Heatis generated by combustion of coal comprising substantially carbonwherein atmospheric oxygen is fed in a continuous stream of fluid airenabling the combustion of carbon in air (or alternatively) pure oxygento produce a continuous stream of carbon dioxide (3) causing thefollowing exothermic reaction:

C+O₂CO₂+Heat [Exothermic reaction];

The above reaction occurs in the presence of all other atmospheric gasescomprising at least 78% nitrogen with other inert atmospheric gases and21% oxygen.

The carbon monoxide component, of the syngas feedstock required for thepresently proposed Fischer-Tropsch reaction synthesizing Fischer-Tropschfluids (including diesel), is most preferably derived by the hightemperature reduction of carbon dioxide (a substantially pure CO₂ gasstream may be derived for use as disclosed herein, by transferring theentire referenced exhaust stream (4) through a membrane gas separationprocess so as to eliminate mostly all other atmospheric gases mostparticularly all atmospheric nitrogen gas (N₂)) combined with addedcarbon particulates no greater than 100 microns across the widestdistance of any particular particle; most preferably, a stream ofheated, pressurized CO₂ gas can be extracted from any suitable exhauststream while it remains at a high temperature, immediately subsequent tothe combustion reaction, via a multiplicity of Inconel conduits, each ofsuitable cross sectional area (about 0.075″ diameter) and heated by anysuitable external means but most preferably by radiant electric heatingarranged around the full outer surface of the Inconel conduit; lowertemperatures will enable the reaction set out below, however, mostpreferably the CO₂ gas is heated to 1,000° C. The hot, exhausted CO₂ gasis transferred through the heated conduit and a suitably proportioned,continuous, pre-heated (to about 1,000° C.) and suitably pressurizedstream of pulverized carbon particles, as described above, mostpreferably within a minimum quantity of carbon dioxide gas, to assist inthe efficient flow of the carbon particulates, at a combined selectedrate of mass flow suitably proportioned so as to enable completereduction of the CO₂ to CO according to the following reaction:

Approx 1,000° C. Heat+C+CO₂→2CO [Endothermic reaction]

Substantially the entire carbon dioxide content of any particularexhaust stream can be converted to carbon monoxide by providing asuitably corresponding quantity of pulverized carbon most preferablysourced from a suitable grade of black coal.

II Production of Hydrogen Gas (2) by Electrolysis of Water

Electrolysis (of water) in an “electrolysis cell,” will decompose waterinto hydrogen gas and oxygen gas which can then be collected separatelywith, in this instance, the hydrogen component provided in acorrespondingly proportioned stream of suitable mass flow to match theabove stream of CO, thereby resulting in a combined relative proportionof CO and H₂ according to a selected value.

It should be noted that to conduct a substantial electric current so asto decompose water at a selected and substantial rate, an electrolyte isrequired to reduce resistance. An electrolysis cell can consist of anelectrode or parallel plate construction utilizing two (or more)electrodes, (preferably manufactured from an inert metal such asplatinum), submerged in an electrolyte. The latter utilizes two or moreplates, also usually an inert metal, with water situated between them,with an electrolyte added.

Electrolysis of water results in the decomposition of water intohydrogen and oxygen as follows:

The electric current disassociates with water molecules into hydroxide(OH⁻) and hydrogen (H⁺) ions.

In the electrolytic cell, hydrogen ions accept electrons in a reductionreaction that forms hydrogen gas at the cathode;

Cathode (reduction): 2H₂O(I)+2e ⁻→H₂(g)+2OH⁻(aq)

At the anode, hydroxide ions undergo an oxidation reaction and give upelectrons to the anode to complete the circuit and form water and oxygengas:

Anode (oxidation): 2H₂O(I)→O₂(g)+4H⁺ (aq)+4e ⁻

hence decomposing water into oxygen and hydrogen;

Overall reaction: 2H₂O(I)→2H₂(g)+O₂(g)

The number of hydrogen molecules produced is therefore twice the amountof oxygen molecules. Assuming equal temperature and pressure for bothgases, the hydrogen gas has twice the quantity of moles as oxygen.

The most commonly used anion is SO₄ ²⁻, as it is very difficult tooxidize.

Standard potential for oxidation of this ion to the peroxydisulfate ionis −0.22 volts.

Frequently used electrolytes:

Strong acids such as Sulfuric acid (H₂SO₄),

2H₂O→2O₂+2H₂ [Endothermic reaction]

In another preferred embodiment a method of manufacturingFischer-Tropsch Fluids of selected formulation can be produced by way of“co-generation,” with the generation of electric power by typical coalfired electricity generating plants which are now most predominantlyinstalled throughout the USA and Canada (and China) such as at Nanitoke,Ontario in CA, or Taylor County, Florida, USA, however, in this instancethe system will be an enclosed loop. Oxygen generated from theelectrolysis of water will be collected and used as the only oxygensource and therefore the reactions will be “balanced” as follows:

C+O₂→CO₂+Heat [Exothermic reaction];

Approx 1,000° C. Heat+C+CO₂→2CO [Endothermic reaction];

Overall electrolysis reaction: 2H₂O(I) 2H₂(g)+O₂(g)

Syngas comprises—2×CO+2×H₂

Carbon fuel comprises—2×C atoms to react with corresponding 2×O atomsderived from electrolysis.

It is also contemplated that in order to generate syngas wherein H₂ andCO are in proportions of 4H2:4 CO; the reactions would therefore be asfollows:

Either 1) or 2);

1) Heat (generated by electrical discharge)+C+CO₂→2CO

2) Or Heat (generated by combustion of C with O₂ derived fromelectrolysis—by the method described below)+3C+O₂+CO₂→4CO

3) 2C+½O₂+CO₂→3CO; or

4) 3C+½O₂+2CO₂→5CO;

NB: The type of reactors which are typically used for this type of hightemperature reaction are generally restricted to about 600° C.-800° C.;The reactor required to enable the reactions proposed in 1) thru 4) willbe facilitated when the conditions provided within the reactor aremaintained at up to 2,000° C. and pressurized up to 5,000 psi;

Such a reactor will require ceramic lining using molded and thermo-setAl₂O₃ (commonly known as Alumina) within a pressure vessel manufacturedfrom a suitably thick Inconel plate,

Wherein the hydrogen and oxygen gas components are generated byelectrolysis, as follows:

5) DC Electricity+2H₂O→2H₂+O₂

One method for generating the H₂ syngas component is described in awhite paper entitled Highly Efficient Hydrogen Generation via WaterElectrolysis Using Nanometal Electrodes by QuantumSphere, Inc., datedSep. 15, 2006.

For purposes of this disclosure, the term “coupled” means the joining oftwo components (electrical or mechanical) directly or indirectly to oneanother. Such joining may be stationary in nature or movable in nature.Such joining may be achieved with the two components (electrical ormechanical) and any additional intermediate members being integrallyformed as a single unitary body with one another or with the twocomponents or the two components and any additional member beingattached to one another. Such joining may be permanent in nature oralternatively may be removable or releasable in nature.

Referring to FIG. 10 a cross section through a cyclone 1015 is shown.The cross section extends in a vertical plane dissecting the verticalcenterline of the apparatus including the connecting upper conduit10144, the lower connecting conduit 10126 and also the horizontalcenterline of the integrated input volute 10107. Insulation panels suchas 10106, 10102, 10121, 10138, 10142, and 10141, are arranged tocompletely enclose the apparatus and high temperature electric heatingelements (providing a suitable means of heating the vessel andconnecting conduits 10144, 10141 and 10126, all enclosed within saidinsulation bats, up to 2,000° C.) which are located at the interfacebetween the insulated panels and the outer surface of the cyclone member10105 and more specifically fixed to the inner surface of the insulationbats such as at 10113 of insulating bat 10106. Therefore, said electricheating elements are located adjacent to the outer surface of saidcyclone member 10105, in very close proximity thereto, however spacedapart there from so as to provide a suitable gap between the heatingelements and the outer surface of said cyclone member 10105 and in sucha manner so as to ensure contact does not occur between the electricheating elements and the cyclone, in spite of their close proximitytogether. The close proximity is most suited to enhancing the effects ofradiated heat from said heating elements which can heat the enclosedmembers up to well above 1,000° C., however, for metal cycloneassemblies this would be a maximum operating temperature for suchmembers manufactured from Inconel (a registered trademark). Said cyclonehas a diameter 10112 (D) as shown by double headed arrow 10135 and thelength of a section of said cyclone 10105 where walls 10116 and 10136are parallel for a distance shown by arrow 10133 and marked at 10114with the letter “L.” A volute 10107 with centerline 10108 is shown atthe upper end of said cyclone 10105 with conduit 10141 connected theretoconveniently so as to provide a means of transferring selected fluids inthe direction shown by arrow 10140; immediately upon transfer aroundpath defined by said volute 10107 as shown by the arrows 10137 whichindicate a direction of fluid flow within the vessel 10105 and in thedirection shown. Conduit 10144 is located at the upper end of member10103 and shares a common centerline with cyclone 10105, extendingupwardly along a perpendicular path, away from cyclone vessel 10105. Atthe lower end of the cyclone member 10105 a smaller conduit 10126 isshown connected directly to the vessel 10105. The sloping sides withinwardly facing walls 10134 and 10120 comprise a lower section of member10105 and the sloping sides allow solid phase particles to be guideddownwardly in the direction shown by arrows 10132 and 10124 therebyproviding a means of directing solid phase ash into the internal spaceof conduit 10126 and downwardly in the direction shown by arrow 10128.In operation the heating elements surrounding the central circularsection 10116 of said cyclone which are mounted closely to said sectionouter surface radiate heat in such a manner as to elevate thetemperature of said cyclone 10105 to approximately 1,000° C. Heat istransferred through the walls of said cyclone 10105 such that when solidparticles that have been carried via conduit 10141 and volute 10110 andat such velocity so as to cause the rotating of matter around the innersurface such as at 10116 and 10136 of said cyclone and in such a mannerthat particles such as carbon which may be carried in a gas such ascarbon dioxide or a vapor such as super heated steam will be heated to acorrespondingly high temperature and when the vapor driving saidparticles is super heated steam, a reaction occurs wherein syngascomprising H₂ and CO is produced. Also, when carbon dioxide is employedas the carbon particle carrier gas, the carbon particles will reactfiercely with the gases provided therein such as carbon dioxide to formcarbon monoxide; most preferably a quantity of hydrogen gas (H₂) will beincluded with CO₂ to inhibit production of coke and deposition thereofonto internal vessel surfaces. When for example, finely granulatedcarbon particles carried by fluid comprising super heated steam, aretransferred in the direction shown by arrow 10140, and then arrows 10137and in such a manner so as to cause rapid rotation of said particlesaround parallel to and in direct contact with the inner surface at 10116and 10136, heat transferred through the wall of vessel 10105 causes aheating of said carbon particles to such an extent that syngascomprising hydrogen and carbon monoxide is formed and then carriedupward, via conduit 10144 in the direction shown by arrows 10103 and10100 through conduit 10144, while ash, which may be produced if saidcarbon particles are impure, is transferred in the direction shown byarrows 10132 and 10124 and then through conduit 10126 in the directionshown by arrow 10128. In this way, finely pulverized carbon particles(<10 micron) can be carried in a fluid/gas such as super heated steam inthe direction shown by arrows and at such a velocity and temperaturethat contact heating enables production of carbon monoxide and hydrogenwhich can be separated from any residual ash derived from impurities inthe carbon particulates. Said syngas transferred via said conduit 10144can then be transferred to a Fischer Tropsch reactor and converted intofluid diesel or other Fischer Tropsch liquids. In another preferredembodiment carbon particles and carbon dioxide are transferred (plushydrogen gas to inhibit carbon production and deposition onto the innersurfaces of containing conduits and vessels) in the direction shown byarrow 10140 and after suitable heating of the carbon particles in thepresence of a suitable catalyst such as nickel aluminite (NiAl) and analkali such as K₂O (Potassium oxide). A reaction between the carbondioxide gas and the carbon particulates will produce carbon monoxideonly, which can then be transferred via conduit 10144 and any residualash transferred via conduit 10126 in the direction shown by arrows10128. Said carbon monoxide gas can then be blended with a measured andproportioned quantity of hydrogen gas which may have been derived fromelectrolysis of water. The production of carbon (coke) can be minimizedwhen the equipment employed to reduce the carbon dioxide to carbonmonoxide has the ability to reduce temperature rapidly after a shortexposure to high temperature and high pressure. The combined gases ofcarbon monoxide and hydrogen gas can be converted to fluid fuels such asdiesel, methanol, jet fuel, and any other suitable selected fuel in aFischer Tropsch reaction. Fuel manufactured in this manner is renewableand can be produced most economically.

Referring now to FIG. 11 the side elevation of various industrialprocesses are represented in diagrammatic format. Processes representedin FIG. 11 include a coal fired electricity generating plant 11106, windturbine 11126 mounted at the top of tower structure 11128 withtransformer 11124 connected to power lines 11122 which in turn connectto electrolysis equipment 11153, in turn connected via gas carryingconduits delivering oxygen to the coal fired plant via 11220 andhydrogen via conduit 11196 to Fischer Tropsch gasification equipment11188, to which syngas carbon monoxide is transferred via conduit 11174in the direction shown by arrow 11168; a Fischer Tropsch reactor 11176is connected via a series of suitably sized conduits to an electricallyheated (via cables 11160) CO₂ reforming apparatus 11189 and the Hydrogenoutput conduit (11136) of equipment 11153 (designed to decompose watervia electrolysis utilizing sulfuric acid (H₂SO₄) electrolyte withelectricity supply from wind turbine 11126 and 11128 via power supplycables 11122).

The American way of life and the associated culture is presently underthreat by the relatively sudden increase in energy costs. Fuel costs arehigher than ever along with related shipping and travel costs; this hastranspired while US coal fired electricity generating plants arestrained to their limits supplying electricity to the US power griddelivering electricity to all major and minor centers of the USA. Theapparent shortage of fluid fossil fuels from American owned sources hastranspired into sudden and significant cost increases with the threat ofever more expensive fossil fuel derived gasoline and diesel is drivingmany endeavors to devise processes for producing renewable fuels such asbiodiesel and ethanol. However opportunities to manufacture diesel fuelin addition to jet fuels from the exhaust streams of electricitygenerating plants, both coal and/or gas fired, are clearly anopportunity that can relieve the upward pressure on gasoline prices andit is a purpose of the present invention to provide a method wherebyrefined Fischer Tropsch processes for fluid fuels production can beemployed in the manufacturing process by the carbon dioxide reforming ofcoal wherein the CO₂ is sourced from exhaust streams emitted from mostcoal fired electricity plants in the USA. It should be noted that a coalfired plant burning some 50,000 tons of coal per day releases some180,000 tons of carbon dioxide into the atmosphere, correspondingly.With the discovery that so called greenhouse gases are detrimentallyaffecting global climate patterns, it is clear that if diesel fuel orany suitable Fischer Tropsch liquid fuel can be manufactured using thecarbon dioxide streams as a major ingredient for a fuel productionsystem could be achieved then this would reduce greenhouse gas emissionswith obvious benefit. The present invention is designed to provide ameans for the production of liquid fuels such as diesel and jet fuelfrom, in major part, carbon dioxide exhaust gases, as described above,emitted, in particular from coal fired electricity generating plants.

The reactions 1) through 3) as set out below represent those in which weare interested and which will enable the recycling of carbon dioxide gasinto Fischer Tropsch liquids where the first (1). Shows carbon monoxideproduction; the second (2). Shows syngas production with a predominanceof hydrogen gas; the hydrogen and carbon monoxide gases (with residualcarbon dioxide and water vapor) is most preferably maintained at aselected temperature and pressure, transferred to a Fischer Tropschreactor containing suitable Nickel, Iron or Cobalt based catalystthereby facilitating the production of a wide range of synthetic dieselformulations and/or “cetane” values plus other Fischer Tropsch liquidswhich can then be separated as needed:

1). Heat**+3C+CO2→2CO+2C; alternatively: Heat**+3C+CO2+H₂→2CO+2C+H₂;

Carbon particles and carbon dioxide maintained at a high temperature (upto 2,000° C.) and high pressure (up to 5,000 psi) are injected into aseries of enclosed ceramic (manufactured from Al₂O₃ otherwise known asalumina) tube sections (tubes are about 0.25″ Diameter arranged end toend and bonded with a suitable adhesive) comprising a total length ofabout 24′ with the ceramic tubes arranged in groupings of for example2×2 (4) tubes which are supported by suitable ceramic members andenclosed within an insulated and water cooled, Inconel tubular profiledpressure vessel. A second 2×2 (4) series of enclosed ceramic tubes ofgreater diameter (1.5″ Dia.) are connected to said first set of (2×2)0.25″ Dia tubes at a confluence and supported also, by suitable ceramicmembers within a continuation of said insulated, water cooled, Inconeltubular profiled pressure vessel with Hydrogen and water injectorsarranged to inject combined, average proportions as shown in 2) below,thereby yielding corresponding proportions of CO and H₂ as shown.

[Heat**; derived from the partial combustion of bio-mass reduced tocarbon particles (or any other suitable source such as by dischargingelectricity via a suitable metal element to generate said heat) andoxygen from atmospheric sources or electrolysis of water—see below—ormost preferably from wind turbine generated electricity which can bedischarged to generate heat in a tightly enclosed and insulatedpressurized vessel];

Hydrogen [derived from # 3) below] and water are injected into reactiontubes at the location indicated above, also a component of hydrogen gasmay be added to the feedstock so as to inhibit coke production and thedeposition thereof onto the catalysts or internal vessel or equipmentsurfaces.

2). Syn-gas production with a predominance ofH₂:-2CO+2H₂0+3H2+2C=4CO+5H₂

3). Electricity*** (Electrolysis)+2H₂0→2H₂+O₂

[Electricity***; generated, most preferably, from wind driven turbines];

Oxygen gas, (O₂ can be derived from any suitable source), in thisinstance generated by way of electrolysis as indicated above, isseparately transferred to a blending station and mixed with a continuousstream of carbon dioxide (derived from exhaust gases) so as to produce ablended gas stream comprising approximately 20% Oxygen and the balanceof approximately 80% Carbon dioxide. The stream of blended gas istransferred to the (for example) combustion chamber of a boiler drivinga steam turbine to drive a suitable generator in electricity production.In this way atmospheric nitrogen is not present in the reactions shownin 1) through 3) above, thereby eliminating production of oxides ofnitrogen which have been associated with damage to the environment onearth.

Syngas as shown in reaction 2) above can then be transferred to aFischer Tropsch reactor with suitable catalysts arranged therein so asto benefit and enhance diesel production.

Referring again to FIG. 11, railroad carriages 11206 and 11204 carryingcoal (or any suitable bio-mass) 11208 and traveling in the directionshown by arrow 11210, are unloaded in building 11104 immediately priorto use to fire steam boilers which in turn drive powers turbine 11106.Exhaust stack 11108 having been capped at 11110 enables the transfer ofall exhaust gases which, after displacement of atmospheric nitrogen gas,is predominantly carbon dioxide or a mixture of carbon dioxide andnitrogen, via conduit 11111 in the direction shown by arrow 11112 andinto steam scrubber 11228. Carbon dioxide having been separated from anyother gases in the exhaust stream, and after scrubbing to remove allunwanted matter such as any traces of sulfur, sodium, calcium or anyother materials etcetera, is transferred in the direction shown by arrow11120 via conduit 11118 and via conduits 11116 in the direction shown byarrow 11114 to compressor 11121. CO2 gases may be chilled and compressedor merely concentrated into heavier vapors but whichever method is used,it is preferable that a flow of dense carbon dioxide gas will be carriedvia conduit 11130 in the direction shown by arrow 11132 and from conduit11130 into reformer equipment via conduit 11152 in the direction shownby arrow 11144. The apparatus shown comprises a series of four ceramicconduits mounted perpendicular to the base chambers 11166 and 11150 aswell as upper chambers 11156 and 11154. Carbon dioxide transferred viaconduit 11152 and into chamber 11150 is combined with a measuredquantity of pulverized carbon having a particulate size less than 5microns so that it can be carried with relative ease in the CO₂ streamvia conduit 11152 and along ceramic conduit 11194 and then into chamber11154. Conduit 11194 and 11192 are manufactured from suitable ceramictube derived from aluminum oxide (AL₂2O₃) and can withstand hightemperatures such as 2,000° C. but cannot tolerate high pressures,therefore, given that most preferably the pressure of gases transferredwith pulverized carbon particles into conduits 11194 and 11192 isbetween 2,000 psi and 5,000 psi the entire apparatus containing saidceramic conduits is enclosed in a pressurized housing shown as members11190, and 11193, which also provides some insulation. Conduits 11192and 11194 are enclosed within insulated segments surrounding each of thetubes and electrical heating elements are arranged to have contact withinsulation and fixing means to the insulation enclosing each conduit.Said heating elements enclosing conduits 11192 and 11194 are arranged inclose proximity to the external surface but are not in direct contacttherewith. In this way radiant heat can be transferred across a smallgap between said conduits and the heating elements and in such a waythat the temperature within said conduits can increase to approximately2000° C. Radiant heating elements are provided and electrical power viacables 11160 with electricity provided, in this instance, by said windturbine 11126 mounted onto column 11128. In this way, electrical energycan be most preferably provided from a wind turbine mounted to column11128 and this energy can then be converted, in effect, to liquid fuel.In another preferred embodiment a measured quantity of oxygen can beprovided via conduit 11152 in the direction shown by arrow 11144 andinto column 11194 after transfer via enclosure 11150. Oxygen provided inthis way can create heat generating combustion within conduit 11194thereby reducing and even eliminating the need for electricity otherwisetransferred via cables 11160. Hot gases and particulates carried intoenclosure 11154 via conduit 11194 are transferred into enclosure 11156before transfer into conduit 11192 within which a pressure of up to5,000 psi and temperature from 1,000° C. and up to 2,000° C. results inthe burning of any remaining oxygen and corresponding quantity of carbonwhich is then converted to carbon dioxide and assuming sufficient carbonis available and then to carbon monoxide prior to transfer intoenclosure 11166, and from there via conduit 11162 in the direction shownby arrow 11164. Gases transferred via conduit 11162 in the directionshown by arrow 11164 will comprise almost entirely carbon monoxide whichis then transferred into Fischer Tropsch vessel 11188 via conduit 11174in the direction shown by arrow 11168. Simultaneously with transfer ofcarbon monoxide gas into vessel 11188, a suitable quantity of hydrogengas is transferred via conduit 11172 in the direction shown by arrow11170 having been derived via electrolysis of water using electrolysisequipment 11153 with water.

Referring to apparatus 11153, which comprises an electrolysis systemcapable of extracting oxygen and hydrogen from water which will mostpreferably contain an electrolyte such as sulphuric acid (H2SO4) orsodium hydroxide (NAOH). Electrolysis apparatus 11153 is provided with asuitable supply of electricity via cables 11122 connected directly witha wind turbine generating electricity. The electrolysis apparatus isessentially divided into two segments, one containing the cathodes, andthe alternate segment containing an anode array. Hydrogen gas collecteddirectly above water contained therein is transferred in the directionshown by arrow 11134 via conduit 11136 in the direction shown by arrow11138. Said hydrogen gas continues via conduit 11196 and 11148 andultimately into conduit 11172 in the direction shown by arrows 11146 and11170. Fischer Tropsch vessel 11188 is maintained at approximately 200°C. and pressurized at up to 4,000 psi and under these conditionsconversion of syngas to diesel and other Fischer Tropsch fluids is mostsuited and 80% of the syngas transferred to vessel 11188 should convertquite readily. Vessel 11188 is provided with a diesel extraction conduitand port 11182 such that diesel fuel can be extracted in the directionshown by 11180 and stored in any suitable storage equipment (not shown)for automotive fuels and then distributed to consumers via existingservice stations, while any remaining gas or “tail gas” is transferredvia conduits 11186 and 11202 in the direction shown by arrows 11200 and11178. Said tail gas can be transferred to the furnace of the coal firedgeneration plant where it will burn readily within the furnace of theelectricity generation plant. It must be noted that in order that theFischer Tropsch reactions to occur in such a balanced way and enableprofit to be made, air cannot be used when providing oxygen tofacilitate combustion within the coal fired boiler at 11106. Instead ablend of about 80% recycled exhaust carbon dioxide and 20% oxygenproduced with the electrolysis of water in apparatus 11153 istransferred via conduit 11234 and 11226 coupled directly to conduit11220 and 11216 to said furnace and boiler 11106 which are isolated fromatmosphere which will therefore eliminate the transfer of nitrogen gasinto the boiler combustion chamber, along with coal 11208 transferredinto power station via carriages 11206 and 11204 in the direction shownby arrow 111210. In this way, electrical energy, which has a very short“life”, can be stored by converting the electrical energy intocontrolled temperature heat and then applying the heat in a manner thatwill facilitate production of fuel by way of chemical reactions alteringthe spent exhaust gases or “medium”, carbon dioxide, which is changed inform to become part of a liquid fuel (or alternatively, gaseous fuel) byconverting spent exhaust (CO₂) into liquid fuel. While exhaust gasesderived from the coal burning generation of electricity is a mostsuitable source of CO₂ for conversion into liquid fuel such as syntheticdiesel, other sources may also be suitable; in particular CO₂ gasgenerated in the normal production of ethanol by fermentation of sugarsextracted from corn is an eminently suitable source and also in theproduction of fossil fuels from crude oil large volumes of CO₂ may bederived. This source is also suitable for use in production of syntheticfuels as described herein. Any source of CO₂ available in sufficientquantity to justify the effort involved may be used as a raw material inthe production of Fischer Tropsch fluids from syngas derived from anysuitable source hydrogen and carbon monoxide derived from CO₂ convertedto carbon monoxide by reforming coal or any carbon source with said CO₂and wherein said hydrogen source can be from electrolysis of water orother source. Electrical power as may be cogenerated according to theprocess described in association with FIG. 11 can be transferred viacable 11102 for use by general industry and for any domestic purposes.

Referring once again to electrolysis apparatus 11153 it should be notedthat purified water is transferred into the electrolysis apparatus viaconduit 11158 in the direction shown by arrow 11232. Any suitableelectrolyte such as sodium hydroxide or sulfuric acid can be blendedtherewith via injection apparatus 11230. All surplus oxygen and alsounwanted synthetic fluids derived from the Fischer Tropsch reactions canbe used to generate electricity by adding to fuel after transfer viaconduits 11202 in the direction of arrow 11200 or via 11214 in thedirection indicated by arrow 11212 and into the plant furnace.

In a preferred embodiment bio-mass in the form of “brewers mash” whichis a by-product of ethanol production can be dehydrated and then used asa normal source of bio-mass material for synthetic diesel production ina similar manner as other bio-mass described above.

Carbon dioxide is generated in the normal fermentation process of cornduring production of ethanol and can therefore be used as a source ofCO₂ gas for production of synthetic diesel as disclosed above.

Corn oil can also be extracted from the brewers mass and used inbio-diesel production as described in association with FIG. 12 below.

Referring now to FIG. 12, cross sections through various members,assembled together to provide a housing enclosing there within twovertically, opposed spring tensioned members. First member 1628 isfabricated from a suitable metal bar such as a 400 series stainlesssteel or high quality carbon tool steel comprising, as would be seen inend view, a round outer perimeter profile with coarse threads 1614machined into a smaller diameter, centrally disposed extension 1735shown in finished machined condition, threaded and attached to member1736 enclosing a series of “O” ring seals such as 1616 provided aroundthe perimeter of shaft 1620. A piston 1602 is fixed rigidly to shaft1620 with cap 1606 suitably machined and attached firmly and fixed inplace to member 1736 enclosing said piston 1602. Hydraulic oil 1612 ofany suitable grade but most preferably of food grade type, fills anenclosed annular space located around shaft 1620 and between member 1736and the under face of piston 1602. Piston 1602 is fitted with anysuitable means of sealing such as “O” rings 1608 and 1610 held captivewithin machined annular slots 1604 and 1609. A pipe 1738 communicatesdirectly between space containing hydraulic oil 1612 and a hydraulic oilpump (not shown) fitted with suitable valves all controlled via asuitably programmed PLC so as to, when and as required, pump oil viaconduit 1740 within pipe 1738 in the directions shown by a first arrow1742 whereby space containing oil 1612 would be reduced in volume andsecondly in the direction shown by arrow 1744 whereby space containinghydraulic oil 1612 would tend to be increased. An opposing and similar,second set of members, attached to said first member 1628 at annularflange 1642 and secured with bolts such as 1636 and 1710 and matchingnuts 1644 and 1712, all adjusted so as to clamp annular flanges 1642 and1646 together in such a manner that a liquid tight seal is created atthe contacting, annular, opposing, intimately contacting faces at 1635.Member 1660 comprises a machined member manufactured from suitable gradebar with hydraulic cylinder 1694 attached rigidly via coarse threads at1696 and 1666 with suitably sized “O” rings 1692 and 1690 arranged so asto be held captive around rod 1670 which in turn is contained within acorresponding suitably drilled and reamed hole 1665. Rod 1670 is fixedrigidly at outermost end to a piston 1682 provided with annular machinedslots 1675 and 1677 within which “O” rings 1684 and 1686 are heldcaptive in such a manner as to provide a liquid tight seal betweenpiston 1682 and piston bore 1674. At the opposite end of rod 1670 amachined and hardened, substantially hemi-spherical profiled member 1656having conically profiled, “flat” faces machined to form the outersurfaces of said hemi-spherical member 1656. A cavity machined intomember 1660 with annular ridges at 1704, 1697, and 1654, is profiled soas to provide contact between all ridges and said conically profiledflat outer surfaces at 1698, 1702, and 1699. A similar set of memberscomprising piston 1602, shaft 1620, and hemi-spherically machined member1630 attached together rigidly and held captive within hemi-sphericallyprofiled aperture with machine ridges 1737 corresponding within flatsurfaces of conically machined segment 1728. A bushing 1729 is suitablymachined and dimensioned so as to fit snugly within annular member 1734.A corresponding bushing also having intimate contact with the innersurface of member 1731 with annular profile arranged to enclose space1650 while allowing members 1713 and 1711 to move in a restricteddirection, parallel to the centerlines of rods 1668 and 1620, of eitheraway from or toward each respective member.

The purpose of the assembled apparatus detailed in association with FIG.12 is to provide a means of thoroughly mixing and homogenizing anycollection and in any relative quantities of fluids, includingtriglycerides as required in bio-diesel production. Springs 1741 heldwithin concentric, circular profiled slots, located within an outerridge such as 1705 are machined in each member 1713 and 1711 arearranged to exert outward pressure against said members 1713 and 1711.Said coiled springs 1741 are arranged to be under constant compression,even in the most relaxed mode and therefore outward pressure resultingin the compression of member 1704 against ridges such as 1697, 1704 and1654 and in correspondingly opposing locations, member 1728 exertspressure against ridges such as 1737 are normal conditions and bypumping high pressurized hydraulic oil into spaces filled by hydraulicoil 1688 and 1612 add even greater pressure to members 1711 and 1713 inan outward direction such that high pressure contact between ridges 1737for example, in member 1628 can be developed. In this way any fluidpumped in the direction shown by arrow 1732 via conduit 1730 or in thedirection shown by arrow 1624 via conduit 1626 can pass via space 1715in the direction shown by arrows 1618 and 1734 only by exertingsufficient pressure to lift member 1713 away from ridges such as ridge1737 thereby allowing said fluid pumped into conduit 1730 to passbetween face 1728 and ridge 1737. Any fluids transferred in this way viaconduit 1730 and/or conduit 1626 will be substantially homogenized andsimilarly any fluids transferred in the direction shown by arrow 1664through conduit 1662 are required to exert sufficient pressure so as tolift member 1711 in the direction shown by arrow 1701 and away fromridges such as 1704, 1697, and 1654, thereby substantially blending andhomogenizing fluids transferred at sufficient pressure between theridges such as 1697 of member 1660 and the flat conical surfaces such as1702 and 1698 of member 1711 to separate the opposing members, allowingtransfer there between.

Any suitable fluid such as triglyceride maintained at a temperatureexceeding 70 degrees F., for example, can be injected, under suitablyhigh pressure (say up to 5,000 psi), so as to be transferred via anyconduit such as 1730, 1626, or via conduit 1662, will be homogenizedafter passing through the homogenizing apparatus shown in FIG. 12.Additional fluid may be transferred in the direction shown by arrow 1634via conduit 1638 and into annular space 1723 and subsequently into space1722, conduit 1718 or 1648, in the direction shown by arrow 1714.Apparatus shown in FIG. 12 can be used to homogenize any suitable fluidsand most appropriately for a combination of fluids including at leastone oil such as a triglyceride mixed with other agents such as ethanolor liquid carbon dioxide. Homogenization of triglycerides is effectivelyachieved by applying a variable and consistent hydraulic pressure withinspaces 1612 and 1688 thereby providing a homogenizing effect to fluidstransferred between member 1713 and 1628 or member 1711 against member1660. Other pressurized fluids transferred via a conduit such as 1726can be mixed thoroughly by transfer through space such as 1722 andsubsequently into conduit 1718 after passing over ridge 1720 which canbe arranged in a tight relationship with opposing depression at theinner end of conduit 1718.

In the manner described in association with FIG. 12 above, any selectedfluids and in particular triglycerides with alcohols, such as ethanol ormethanol, can be thoroughly mixed together and homogenized in such a waythat will ensure the mixed condition, necessary in bio-dieselproduction, remains for sufficient time to allow reactions to occur soas to produce bio-diesel while held under a pressure of approximately2,500 psi to 5,000 psi and at a selected and suitable temperature suchas about 260° C.

The present disclosure has been described with reference to exampleembodiments, however workers skilled in the art will recognize thatchanges may be made in form and detail without departing from the spiritand scope of the disclosure. For example, although different exampleembodiments may have been described as including one or more featuresproviding one or more benefits, it is contemplated that the describedfeatures may be interchanged with one another or alternatively becombined with one another in the described example embodiments or inother alternative embodiments. Because the technology of the presentdisclosure is relatively complex, not all changes in the technology areforeseeable. The present disclosure described with reference to theexample is manifestly intended to be as broad as possible. For example,unless specifically otherwise noted a single particular element may alsoencompass a plurality of such particular elements.

It is also important to note that the construction and arrangement ofthe elements of the system as shown in the preferred and other exemplaryembodiments is illustrative only. Although only a certain number ofembodiments have been described in detail in this disclosure, thoseskilled in the art who review this disclosure will readily appreciatethat many modifications are possible (e.g., variations in sizes,dimensions, structures, shapes and proportions of the various elements,values of parameters, mounting arrangements, use of materials, colors,orientations, etc.) without materially departing from the novelteachings and advantages of the subject matter recited. For example,elements shown as integrally formed may be constructed of multiple partsor elements shown as multiple parts may be integrally formed, theoperation of the assemblies may be reversed or otherwise varied, thelength or width of the structures and/or members or connectors or otherelements of the system may be varied, the nature or number of adjustmentor attachment positions provided between the elements may be varied. Itshould be noted that the elements and/or assemblies of the system may beconstructed from any of a wide variety of materials that providesufficient strength or durability. Accordingly, all such modificationsare intended to be included within the scope of the present disclosure.Other substitutions, modifications, changes and omissions may be made inthe design, operating conditions and arrangement of the preferred andother exemplary embodiments without departing from the spirit of thepresent subject matter.

1. A method for the production of a bio-diesel fuel from bio-mass, themethod comprising: (a) providing a quantity of bio-mass; (b) combiningthe biomass with CO₂ and ethanol, methanol, or a combination thereof ina catalyst-lined channel at a temperature of at least 80° C. and apressure of at least 1000 psia to form a mixture of bio-diesel andglycerol; (c) separating the glycerol from the bio-diesel.
 2. The methodof claim 1 further comprising the various aspects of the embodimentsdisclosed in the specification.